Hydrogenation processes

ABSTRACT

The present invention is directed to a process for hydrogenating one or more organic compounds especially unsaturated organic compounds by bringing the compound into contact with a hydrogen-containing gas in the presence of a catalyst, which comprises one or more catalytically active metals applied to a porous catalyst support. The one or more catalytically active metals having been derived via a decomposed organic complex of the metal on the support, in particular amine complexes of the metal. The decomposed complex may be treated with hydrogen to activate the catalyst before use as a hydrogenation catalyst.

This application is the National Stage of International Application No.PCT/EP03/12885, filed Nov. 18, 2003, which claims the benefit of GreatBritain Application 0227086.6, filed Nov. 20, 2002, the entiredisclosures of which are hereby incorporated herein by reference.

FIELD OF INVENTION

The present invention relates to a process for the hydrogenation oforganic compounds and to a process for the manufacture of ahydrogenation catalyst and in particular to a hydrogenation process thatutilizes a hydrogenation catalyst prepared via the formation anddecomposition of an organic complex on a catalyst support.

BACKGROUND OF THE INVENTION

Hydrogenation is an established process both in the chemical andpetroleum refining industries. Hydrogenation is conventionally carriedout in the presence of a catalyst, which usually comprises a metalhydrogenation component deposited on a porous support material. Themetal hydrogenation component is often one or more metals for examplenickel, platinum, palladium, rhodium, ruthenium or mixtures thereof.

Many organic compounds have one or more groups or functionality that issusceptible to hydrogenation under appropriate conditions with the useof a suitable metal containing catalyst. One particular group ofcompounds that are susceptible to hydrogenation is those that containone or more unsaturated groups or functionality such as for examplecarbon-carbon double bonds or triple bonds.

Hydrogenated derivatives of benzenepolycarboxylic acids or derivativesthereof, such as esters and/or anhydrides, have many uses. Of particularinterest is their use as plasticisers for polymeric materials. In thiscontext the dialkylhexahydrophthalates are an example of one class ofthese compounds that are of particular interest. These materials may beproduced by hydrogenation of the corresponding phthalic acid ester inthe presence of hydrogen and an active metal hydrogenation catalystdeposited on a support.

In U.S. Pat. No. 5,286,898 and U.S. Pat. No. 5,319,129,dimethylterephthalate is hydrogenated at ≧140° C. and a pressure of from50 to 170 bar over supported Pd catalysts, which are treated with Ni, Ptand/or Ru to give the corresponding dimethylhexahydroterephthalate. Thesupports used are alumina of crystalline phase alpha or theta or deltaor gamma or beta or mixtures thereof.

In EP-A-0 005 737, aromatic carboxylic esters are hydrogenated at from70 to 250° C. and from 30 to 200 bar over supported Ni, Ru, Rh and/or Pdcatalysts to give the corresponding cycloaliphatic carboxylic esters.The support used is an aluminium oxide of which at least 20% has beenconverted into lithium-aluminium spinel.

U.S. Pat. No. 3,027,398 describes the hydrogenation ofdimethylterephthalate over supported Ru catalysts at from 110 to 140° C.and from 35 to 105 bar. The Ru is deposited on charcoal or kieselguhr.

EP-A 0 603 825 relates to a process for the preparation of1,4-cycylohexanedicarboxylic acid by hydrogenating terephthalic acid byusing a supported palladium catalyst, wherein as support alumina, silicaor active charcoal is used.

U.S. Pat. No. 3,334,149 describes a multistage process for thehydrogenation of dialkylterephthalate using a Pd catalyst followed byuse of a copper chromite catalyst.

U.S. Pat. No. 5,936,126 describes a process for the hydrogenation of anaromatic compound. The catalyst used contains ruthenium as active metalalone or optionally with one or more other Group IB, VIIB or VIIIBmetals on a macroporous support. The macroporous support exhibits anaverage pore diameter of at least 50 nm and a BET surface area of notmore than about 30 m²/g.

U.S. Pat. No. 6,248,924 describes a process for reacting organiccompounds. The catalyst used contains ruthenium as active metal alone oroptionally with one or more other Group IB, VIIB or VIIIB metals on asupport. The support may be a material having macropores (50 to 10000 nmpore diameter) and mesopores (2 to 50 nm pore diameter). In the support10-50% of the pores are macropores and 50 to 90% of the pores aremesopores. Alumina of surface area (BET) 238 m²/g is specificallyexemplified.

Published International Application No. PCT/EP98/08346 (WO 99/32427)describes a process for the hydrogenation of benzene polycarboxylicacids or derivatives thereof. The catalyst used comprises ruthenium asan active metal which is deposited alone or together with at least oneother metal of subgroups I, VII or VIII of the periodic table on asupport. One of three separate types of support may be used. The firstsupport is macroporous having a mean pore diameter of at least about 50nm and a BET surface area of at most 30 m²/g. The second support is amaterial, which has both macropores and mesopores (2 to 50 nm porediameter), and in which 5-50% of the pores are macropores, 50 to 95% ofthe pores are mesopores and the surface area of the support ispreferably from 50 to about 500 m²/g. The third type of support is amaterial, which is macroporous and has a mean pore diameter of at least50 nm and a surface area of at most 15 m²/g.

Of particular importance in all hydrogenation processes is the degree ofconversion of the starting materials and the selectivity of conversioninto the desired hydrogenated products. The degree of conversion andselectivity should be as high as possible. In addition it is highlydesirable to develop hydrogenation processes that proceed at acceptablereaction rates.

There is a need therefore for efficient hydrogenation processes for thehydrogenation of organic compounds and in particular for thehydrogenation of unsaturated compounds such as for example aromaticcompounds to the corresponding ring-hydrogenated derivatives, whichprocesses are highly selective and proceed at good reaction rates. It istherefore an object of the present invention to provide a process forhydrogenating organic compounds to hydrogenation products with highlevels of conversion, selectivity and with good rates of reaction, andto provide a hydrogenation catalyst for use in such a hydrogenationprocess and to a process for the manufacture of such a hydrogenationcatalyst.

SUMMARY OF THE INVENTION

The present invention accordingly provides a process for hydrogenatingone or more organic compounds, which process comprises bringing the oneor more organic compound into contact, under hydrogenation conditions,with a source of hydrogen in the presence of a catalyst comprising oneor more catalytically active metal sites located on a catalyst supportand recovering the hydrogenation products, wherein at least one of thecatalytically active metal sites has been obtained via the decompositionon the support of an organic complex of the metal.

In a further aspect the present invention also provides a process forhydrogenating one or more benzenepolycarboxylic acids or one or morederivatives thereof, or a mixture of one or more benzenepolycarboxylicacids with one or more derivatives thereof by bringing, underhydrogenation conditions, the benzenepolycarboxylic acid or thederivative thereof or the mixture into contact with ahydrogen-containing gas in the presence of a catalyst, the catalystcomprising one or more catalytically active metal sites located on acatalyst support, wherein at least one of the catalytically active metalsites has been obtained via decomposition on the support of an organiccomplex of the metal.

In a further aspect the present invention also provides a process forthe manufacture of a hydrogenation catalyst which process comprises;

-   -   a) preparing a support having one or more organic complexes of        one or more catalytically active metals located thereon; and    -   b) decomposing one or more of the organic metal complexes        located on the support.

In a further aspect the present invention also provides for ahydrogenation catalyst comprising one or more catalytically activemetals and one or more support materials wherein the total metaldispersion is 45% or more and the metal dispersion relating to astrongly chemisorbed component of the total metal dispersion is 20% orgreater.

In a further embodiment of each aspect of the present invention theorganic complex on the support is partially decomposed.

In a further embodiment of each aspect of the present invention theorganic complex on the support is fully decomposed.

In a further embodiment of each aspect of the present invention fulldecomposition may be achieved by exposing the organic complex on thesupport to pyrolysis conditions in the presence of hydrogen.

In a further embodiment of each aspect of the present invention thedecomposition of the organic metal complex is followed by treatment ofthe fully or partially decomposed organic complex on the support with asource of hydrogen. When the hydrogen treatment is of a partiallydecomposed organic complex on the support the hydrogen treatmentpreferably fully decomposes the partially decomposed organic complex.

BRIEF DESCRIPTION OF THE DRAWINGS

The present invention will be better understood by reference to theDetailed Description of the Invention when taken together with theattached drawings wherein:

FIG. 1 shows a plot of DINP conversion vs reaction time for 0.5 wt %Ru/MCM-41 catalyst in which the active metal has been deposited from anaqueous solution, and

FIG. 2 shows a plot of DINP conversion vs reaction time for 0.5 wt %Ru/MCM-41 catalyst in which the active metal has been deposited from amixture of an aqueous solution of metal with triethanolamine.

FIG. 3 shows a quadrapole mass spectrum of the product of Example 7heated in air at 4 deg/min,

FIG. 4 shows the transmission infra-red spectra of silica and Examples7, 9 and 14,

FIG. 5 shows an air treatment TGA plot for a supported metal catalyst(0.5 wt % Ru/SiO₂) prepared using impregnation of the metal withtriethanolamine and drying at 100° C.,

FIG. 6 shows an air treatment TGA plot for a supported metal catalyst(0.5 wt % Ru/SiO₂) prepared using impregnation of the metal withtriethanolamine and calcination at 300° C., and

FIG. 7 shows a hydrogen treatment TGA plot for a supported metalcatalyst (0.5 wt % Ru/SiO₂) prepared using impregnation of the metalwith triethanolamine and calcination at 300° C.

DETAILED DESCRIPTION OF THE INVENTION

In the process of the present invention organic compounds especiallyunsaturated organic compounds are hydrogenated in the presence ofhydrogen and a hydrogenation catalyst that has been prepared in aspecific way. The hydrogenation catalyst is prepared via the formationof one or more organic metal complexes, as the source of catalyticallyactive metal. After deposition and/or formation of one or more organicmetal complexes in or on the support material the complexes arepartially or fully decomposed. This method of preparation results inhydrogenation catalysts that have good catalytic activity when comparedto hydrogenation catalysts prepared using more conventional catalystpreparation methods. We have found that when at least one of the activehydrogenation metals is deposited in this way the resultant catalyst ishighly active in hydrogenation processes. In a further embodiment thefully or partially decomposed organic complex is treated in a furtherstage with a source of hydrogen. This further stage may be omitted whena hydrogen source is used in a first stage to fully decompose theorganic complex.

The process of the present invention is suitable for hydrogenating anyorganic compound that is susceptible to hydrogenation. Organic compoundsthat are particularly suitable are organic compounds that comprise oneor more groups or functionality with unsaturated bonds; these compoundsare herein described as “unsaturated organic compounds”. The term“unsaturated organic compound” as used within the present inventioncomprises all organic compounds including low molecular weight(monomeric) and polymeric organic compounds which may be catalyticallyreacted, in particular those which exhibit groups which are treatablewith hydrogen, such as carbon-carbon double or carbon-carbon triplebonds. This term comprises low molecular weight organic compounds aswell as polymers. “Low molecular weight organic compounds” are compoundshaving a molecular weight of below 500. The term “polymer” is defined asrelating to molecules having a molecular weight of higher than about500.

In particular, organic compounds having one or more of the followingstructural units may be used, although the present invention is notlimited to organic compounds that only have these structural units asgroups that are susceptible to hydrogenation.

The process of the invention is particularly suitable for hydrogenatingan unsaturated organic compound which is selected from the groupconsisting of an aromatic compound in which at least one hydroxyl groupis bonded to an aromatic ring, an aromatic compound in which at leastone amino group is bonded to an aromatic ring, an aromatic compound inwhich at least one carboxylic acid group or derivative thereof is bondedto an aromatic ring, a ketone, an aldehyde, a carboxylic acid or aderivative thereof, a polymer comprising at least one carbon-carbondouble bond, a polymer comprising at least one carbonyl group, a polymercomprising at least one nitrile group, and a mixture of two or morethereof. Aliphatic unsaturated organic compounds comprising aldehydegroups as the only unsaturated group are not preferred. Aliphaticunsaturated organic compounds comprising aldehyde groups and alcoholgroups especially polyols such as D-glucose are not preferred.

Within the process of the invention unsaturated organic compoundscomprising units of different structures, as defined above, may behydrogenated, such as unsaturated organic compounds, which exhibitcarbon-carbon multiple bonds and carbonyl groups, since the catalystused within the process of the invention are capable to firstselectively hydrogenate one of the two groups, i.e. to achieve ahydrogenation of these groups from about 90 to 100%, while at first theother groups are reacted, preferably hydrogenated, to an extent of lessthan 25% and in general 0 to about 7%. Generally, first thecarbon-carbon multiple bond and subsequently the nitrile group arereacted, e.g. hydrogenated, respectively.

The term “aromatic compound in which at least one hydroxyl group isbonded to an aromatic ring” or “aromatic compound in which at least oneamino group is bonded to an aromatic ring” or “aromatic compound inwhich at least one carboxylic acid group or derivative thereof is bondedto an aromatic ring” means all compounds which have a unit of thestructure (I):

wherein R is a hydroxyl group or an amino group or carboxylic acid groupor derivative thereof. In structure (I) there may be two or moresubstituent R groups in the aromatic ring.

If, in the process of the present invention, use is made of aromaticcompounds in which at least one hydroxyl group and also at least oneunsubstituted or substituted C₁-C₁₀-alkyl radical and/or C₁-C₁₀-alkoxyradical is bonded to an aromatic ring, the resulting isomer ratio of cisto trans products can be varied within a wide range, depending on thereaction conditions (temperature, solvent). Furthermore, the compoundsobtained can be processed further without further purification steps,since the formation of alkylbenzenes is virtually completely avoided.

Like the above-described compounds in which at least one hydroxyl groupis bonded to an aromatic ring, aromatic compounds in which at least oneamino group is bonded to an aromatic ring can also be hydrogenated bythe process of the present invention to give the correspondingcycloaliphatic compounds with high selectivity. For the aminesadditionally substituted by a C₁-C₁₀-alkyl radical and/or C₁-C₁₀-alkoxyradical, what has been said above regarding the ratio of the cis andtrans isomers also applies.

In particular, this embodiment substantially avoids the formation ofdeamination products such as cyclohexanes or partially hydrogenateddimerization products such as phenylcyclohexylamines. In detail, thefollowing compounds may be hydrogenated with the process of theinvention.

Aromatic compounds in which at least one hydroxyl group and preferablyalso at least one unsubstituted or substituted C₁-C₁₀-alkyl radicaland/or alkoxy radical is bonded to an aromatic ring can be hydrogenatedby means of the process of the present invention to give thecorresponding cycloaliphatic compounds, with it also being possible touse mixtures of two or more of these compounds. The aromatic compoundsused can be monocyclic or polycyclic aromatic compounds. The aromaticcompounds contain at least one hydroxyl group bonded to an aromaticring; the simplest compound of this group is phenol. The aromaticcompounds preferably have one hydroxyl group per aromatic ring and canbe substituted on the aromatic ring or rings by one or more alkyl and/oralkoxy radicals, preferably C₁-C₁₀-alkyl and/or alkoxy radicals,particularly preferably C₁-C₁₀-alkyl radicals, in particular methyl,ethyl, propyl, isopropyl, butyl, isobutyl and tert-butyl radicals; amongthe alkoxy radicals, preference is given to C₁-C₈-alkoxy radicals suchas the methoxy, ethoxy, propoxy, isopropoxy, butoxy, isobutoxy andtert-butoxy radicals. The aromatic ring or rings and also the alkyl andalkoxy radicals may be unsubstituted or substituted by halogen atoms, inparticular fluorine atoms, or other suitable inert substituents.

Preferably, the compounds which can be hydrogenated according to thepresent invention have at least one, preferably from one to four, inparticular one, C₁-C₁₀-alkyl radical which is preferably located on thesame aromatic ring as the hydroxyl group or groups. Preferred compoundsare (mono)alkylphenols, where the alkyl radical can be in the o, m or pposition relative to the hydroxyl group. Particular preference is givento trans-alkylphenols, also known as 4-alkylphenols, where the alkylradical preferably has from 1 to 10 carbon atoms and is, in particular,a tert-butyl radical. Preference is given to 4-tert-butylphenol.Polycyclic aromatic compounds, which can be used according to thepresent invention are, for example, β-naphthol and α-naphthol.

The aromatic compounds in which at least one hydroxyl group andpreferably also at least one unsubstituted or substituted C₁-C₁₀-alkylradical and/or alkoxy radical is bonded to an aromatic ring can alsohave a plurality of aromatic rings which are linked via an alkyleneradical, preferably a methylene group. The alkylene group, preferablymethylene group, which forms the linkage can have one or more alkylsubstituents which can be C₁-C₂₀-alkyl radicals and are preferablyC₁-C₁₀-alkyl radicals, particularly preferably methyl, ethyl, propyl,isopropyl, butyl or tert-butyl.

In these compounds, each of the aromatic rings can bear at least onebonded hydroxyl group. Examples of such compounds are bisphenols, whichare linked in the 4 position via an alkylene radical, preferably amethylene radical.

In the process of the present invention, particular preference is givento reacting a phenol substituted by a C₁-C₁₀-alkyl radical, preferablyC₁-C₆-alkyl radical, where the alkyl radical may be unsubstituted orsubstituted by an aromatic radical, or mixtures of two or more of thesecompounds. In a further preferred embodiment of this process,p-tert-butylphenol, bis(p-hydroxyphenyl) dimethylmethane or a mixturethereof is hydrogenated.

The process of the present invention also enables aromatic compounds inwhich at least one amino group is bonded to an aromatic ring to behydrogenated to give the corresponding cycloaliphatic compounds, withmixtures of two or more of these compounds also being able to be used.The aromatic compounds can be monocyclic or polycyclic aromaticcompounds. The aromatic compounds contain at least one amino group,which is bonded to an aromatic ring. The aromatic compounds arepreferably aromatic amines or diamines and can be substituted on thearomatic ring or rings or on the amino group by one or more alkyl and/oralkoxy radicals, preferably C₁-C₂₀-alkyl radicals, in particular methyl,ethyl, propyl, isopropyl, butyl, isobutyl and tert-butyl radicals. Amongthe alkoxy radicals, preference is given to C₁-C₈-alkoxy radicals suchas methoxy, ethoxy, propoxy, isopropoxy, butoxy, isobutoxy andtert-butoxy radicals. The aromatic ring or rings and also the alkyl andalkoxy radicals can be unsubstituted or substituted by halogen atoms, inparticular fluorine atoms, or other suitable inert substituents.

The aromatic compound in which at least one amino group is bonded to anaromatic ring can also have a plurality of aromatic rings which arelinked via an alkylene group, preferably a methylene group. The alkylenegroup, preferably methylene group, which forms the linkage can bear oneor more alkyl substituents which can be C₁-C₂₀-alkyl radicals and arepreferably C₁-C₁₀-alkyl radicals, particularly preferably methyl, ethyl,propyl, isopropyl, butyl, sec-butyl or tert-butyl. The amino groupbonded to the aromatic ring may be unsubstituted or substituted by oneor two of the above-described alkyl radicals. Particularly preferredcompounds are aniline, naphthylamine, diaminobenzenes, diaminotoluenesand bi-p-aminophenylmethane or mixtures thereof.

Within the process of the invention it is also possible to react, inparticular to hydrogenate, compounds comprising carbonyl groups, i.e. inparticular aldehydes, ketones, carboxylic acids and their derivatives,such as carboxylic acid esters, carboxylic acid halides and carboxylicanhydrides, and mixtures of two or more of the above-mentionedcompounds.

In particular aldehydes and ketones, preferably those having 1 to 20C-atoms, such as formaldehyde, acetaldehyde, propionaldehyde,n-butyraldehyde, valeraldehyde, caproaldehyde, heptaldehyde,phenylacetaldehyde, acrolein, crotonaldehyde, benzaldehyde, o-, m-,p-tolualdehyde, salicylic aldehyde, anisaldehyde, vanillin, zinnamicaldehyde, acetone, methyl ethyl ketone, 2-pentanone, 3-pentanone,2-hexanone, 3-hexanone, cyclohexanone, isophorone, methyl isobutylketone, mesityl oxide, acetophenone, propiophenone, benzophenone,benzalacetone, dibenzalacetone, benzalacetophenone, glycol aldehyde,glyoxal, 2,3-butandione, 2,4-pentandione, 2,5-hexandione,terephthalaldehyde, glutaraldehyde, diethylketone, methyl vinyl ketone,acetylacetone, 2-ethylhexanal, or mixtures of two or more thereof, maybe used.

Furthermore, also polyketones, such as copolymers of ethylene and CO areused.

Furthermore, carboxylic acids and derivatives thereof, preferably thosehaving 1 to 20 C-atoms may be reacted. In particular, the following areto be mentioned: Carboxylic acids, such as formic acid, acetic acid,propanoic acid, butanoic acid, iso-butanoic acid, n-valeric acid,pivalic acid, caproic acid, heptanoic acid, octanoic acid, decanoicacid, lauric acid, myristic acid, palmitic acid, stearic acid, acrylicacid, methacrylic acid, oleic acid, elaidic acid, linoleic acid,linolenic acid, cyclohexane carboxylic acid, benzoic acid, phenylaceticacid, o-, m-, p-toluylic acid, o-, p-chlorobenzoic acid, o-,p-nitrobenzoic acid, salicylic acid, p-hydroxybenzoic acid, anthranilicacid, p-aminobenzoic acid, oxalic acid, malonic acid, succinic acid,glutaric acid, adipic acid, pimelic acid, suberic acid, azelaic acid,sebacic acid, maleic acid, fumaric acid, phthalic acid, isophthalicacid, terephthalic acid, trimellitic acid, trimesic acid, pyromelliticacid, hemimellitic acid and mixtures of two or more thereof.

Carboxylic acid halides, such as the chlorides and bromides of theabove-mentioned carboxylic acids, in particular acetylchloride or-bromide, stearic acid chloride or -bromide and benzoic acid chloride or-bromide, which are dehalogenated.

Carboxylic acid esters, such as the C₁- to C₁₀-alkyl esters of theabove-mentioned carboxylic acids, particularly methyl formate, aceticacid ester, butanoic acid butyl ester, dimethyl terephthalate, dimethyladipate, methyl (meth)acrylate, butyrolactone, caprolactone andpolycarboxylic acid esters, such as polyacrylic and polymethacrylic acidesters and copolymers and polyesters thereof, such aspoly(methyl(meth)acrylates); these esters are in particularhydrogenated, i.e. the esters are reacted to the corresponding acids andalcohols.

Carboxylic anhydrides, such as anhydrides of the above-mentionedcarboxylic acids, in particular acetic acid anhydride, propanoic acidanhydride, benzoic acid anhydride and maleic anhydride.

Carboxylic acid amides, such as amides of the above-mentioned carboxylicacids, such as formamide, acetamide, propionic amide, stearamide andterephthalamide.

In addition thereto, also hydroxy carboxylic acids, such as lactic,malic acid, tartaric acid or citric acid, or amino acids, such asglycine, alanine, proline and arginine may be reacted.

Furthermore, also nitrites, preferably aliphatic or aromatic mono ordinitriles, such as acetonitrile, propionitrile, butyronitrile, stearicacid nitrile, isocrotonic acid nitrile, 3-butylnitrile, 2,3-butadienenitrile, 2,4-pentadiene nitrile, 3-hexene-1,6-dinitrile,chloracetonitrile, trichloracetonitrile, lactic acid nitrile, phenolacetonitrile, 2-chlorbenzonitrile, 2,6-dichlorobenzonitrile,isophthalonitrile, particularly aliphatic alpha, omega-dinitriles, suchas succinonitrile, glutaronitrile, adiponitrile, pimelicnitrile andsuberic nitrile or aminonitriles, such as 4-amino butanoic acid nitrile,5-aminopentanoic acid nitrile, 6-aminohexanoic acid nitrile,7-aminoheptanoic acid nitrile and 8-aminooctanoic acid nitrile.

Furthermore, within the process according to the invention, thefollowing reactions may be carried out: The hydrogenation of aromaticcompounds, such as benzene, toluenes, xylols, naphthalines andsubstituted derivatives thereof, leading to the corresponding alicyliccompounds; the hydrogenation of alkenes or alkynes, such as ethylene,propylene, 1-, 2-butene, 1-, 2-, 3- and 4-octene, butadiene, andhexatriene leading to the corresponding alkanes; the hydrogenation ofnitroalkanes, such as nitroethane, nitromethane, nitropropane and1,1-dinitroethane leading to the corresponding amines; the hydrogenationof imines, such as quinone imines, ketimines, ketene imines or aliphaticimines, such as propioamine, hexane imine; the dehalogenation or organiccompounds which contain halogen atoms, particularly of aromatichalogen-containing compounds, such as chloro- and bromobenzene, bromo-and chlorotoluenes and chloro- and bromo xylols, also includingcompounds with more than one halogen atoms substituted, may be used; theaminating hydrogenation of i.e. alcohols, such as vinyl alcohol.Furthermore, within the process of the invention also oximes may behydrogenated.

The catalysts according to the invention may be also used for thehydrogenation of large molecules, preferably of polymers. Accordingly,the present invention also relates to a process for hydrogenating apolymer comprising at least one catalytically reactable group in thepresence of the above identified catalyst, wherein the hydrogenation ofpolymers comprising carbonyl groups, such as polyesters of dicarboxylicacids, unsaturated monocarboxylic acids, such as poly(meth)acrylates,olefin/CO-copolymers or polyketones, and the hydrogenation of polymerscomprising nitrile groups, such as copolymers of styrene and butadiene,copolymers of acrylonitrile and the aminating hydrogenolysis ofpolyvinylalcohols and polyketones in the presence of the above-mentionedcatalyst are preferred.

In particular, the present invention relates to a process for thehydrogenation of a polymer comprising at least one carbonyl group or apolymer comprising at least one nitrile group.

The term “polymer comprising at least one catalytically reactable group”relates to all polymers comprising such groups, in particular topolymers comprising units having the structures (I) to (VIII), asdefined above with respect to the monomeric compounds, or a halogenatom. Needless to say that the referenced polymers comprise therespective unit at least once and that also one or more units of two ormore of said structures may be present in the polymer reacted accordingto the invention.

The average molecular weight of the polymers to be reacted within theprocess of the invention is generally about 500 to about 500000,preferably about 1000 to about 100000 and more preferably about 1000 toabout 50000. It is, however, possible to also react polymers having ahigher molecular weight of up to one or several millions. If polymerscomprising at least one carbon-carbon multiple bond, i.e. polymerscomprising repeating units of the above defined structures (I) and (II)are reacted, these generally exhibit a weight average molecular weightof from about 5000 to about 1000000, preferably from about 50000 toabout 500000 and more preferably from about 150000 to about 500000.

It is preferred to use polymers containing olefinic double bonds, and itis further preferred to use polymers containing diene units andcopolymers containing vinylaromatic units and diene units. Within thisreaction besides the catalyst comprising ruthenium as the active metal,also the catalyst comprising palladium as the active metal may be used.Common diene units include all conventional polyunsaturated monomerscontaining from three to twelve carbon atoms, butadiene being preferred.Copolymers to be hydrogenated may contain recurring units in random,block, or tapered distribution.

Aromatic monomers, which may be present in the polymers to behydrogenated in the process of the invention, includemonovinyl-substituted and polyvinyl-substituted aromatic compounds, thepreferred monomers being styrene, alpha-methyl styrene, acrylonitrile,methacrylonitrile, and divinyl benzene. Furthermore, mixtures ofvinylaromatic and/or diolefin monomers, optionally together withconventional olefinic monomers, can be present in the polymers to behydrogenated.

As examples for polymers which may be hydrogenated with the process ofthe invention the following are to be mentioned: polymers havingcarbon-carbon double bonds, e.g. polybutadienes, such aspoly(2,3-dimethylbutadiene), polyisoprene, polyacetylenes andpolycylopenta- and -hexadiene; polymers having carbon-carbon triplebonds, such as polydiacetylenes; polymers having aromatic groups, suchas polystyrene, terpolymers of acrylonitrile, butadiene and styrene, andcopolymers of styrene and acrylonitrile; polymers having carbon-nitrogentriple bonds, such as polyacrylonitrile, polyacrylonitrile-copolymerswith e.g. vinyl chloride, vinylidene chloride, vinyl acetate or(meth)acrylic acid esters or mixtures of two or more thereof ascomonomers; polymers having carbon-oxygen double bonds, such aspolyesters, polyacrylamides, poly(acrylic acids), polyurea andpolyketones; polymers having carbon-sulfur double bonds, such aspolysulfones and polyethersulfones; halogen-containing polymers, such aspoly(vinyl chloride) and poly(vinylidene chloride); and polymerscontaining nitro groups, which may be obtained by nitration of e.g.polyolefins by means of polymer analogous reactions.

Examples for polymers being preferably used within the present inventioninclude polyisoprene, polybutadiene, ethylene/CO-copolymers,propylene/CO-copolymers, poly(methyl(meth)acrylate), polyterephthalate,polyadipate, styrene-butadiene-copolymers,acrylonitrile-butadiene-copolymers, acrylonitrile-styrene-copolymers,styrene-isoprene-styrene-triblock copolymers,styrene-butadiene-styrene-triblock copolymers andstyrene-butadiene-styrene-starblock copolymers.

Generally, a complete reaction of the introduced compounds is achieved.However, the reaction, preferably hydrogenation, may also be carried outin such a way that by suitably choice of temperature, H₂-pressure and/orH₂-amount only one of the type of groups susceptible to hydrogenationmay be reacted, while the other kind of groups susceptible tohydrogenation are not appreciably hydrogenated.

The process of the invention is particularly suitable hydrogenatingpolymers comprising units of different structure, as defined above, e.g.a polymer comprising carbon-carbon multiple bonds and carbonyl groupsand/or nitrile groups, since the catalyst of the present invention iscapable to first selectively react the carbon-carbon multiple bond, e.g.to achieve a hydrogenation of these groups of about 90 to 100%, while atthe same time the carbonyl groups and/or nitrile groups are reacted,e.g. hydrogenated to an extent of less than 25% and in general 0 toabout 7%.

Furthermore, the process of the invention is particularly suitable forthe hydrogenation of polymers of high molecular weight and containingboth carbon-carbon multiple bonds and aromatic groups, since thecatalysts used in the process of the invention are capable of achievinghydrogenation of the carbon-carbon multiple bonds, e.g. ethylenicallyunsaturated regions, to an extent of from 90 to 100%, whilst thearomatic regions are hydrogenated to an extent of less than 25% andgenerally to an extent of from 0% to 7%.

After finishing this reaction, preferably hydrogenation of thecarbon-carbon multiple bonds, it is of course possible to nearlyquantitatively react, preferably hydrogenate, the other unsaturatedgroups being present in the polymer, e.g. carbonyl groups by furtherintroducing hydrogen. The process of the invention may be used foralready isolated and living polymers.

The process of the present invention is of particular benefit in thehydrogenation of benzenepolycarboxylic acid or a derivative thereof,which are the most preferred organic compound for hydrogenation in theprocess. The term “benzenepolycarboxylic acid or a derivative thereof”used for the purposes of the present invention encompasses allbenzenepolycarboxylic acids as such, e.g. phthalic acid, isophthalicacid, terephthalic acid, trimellitic acid, trimesic acid, hemimelliticacid and pyromellitic acid, and derivatives thereof, particularlymonoesters, diesters and possibly triesters and tetraesters, inparticular alkyl esters, and anhydrides such as phthalic anhydride andtrimellitic anhydride or their esters. The esters used are alkyl,cycloalkyl and alkoxyalkyl esters, where the alkyl, cycloalkyl andalkoxyalkyl groups generally have from 1 to 30, preferably from 2 to 20and particularly preferably from 3 to 18, carbon atoms and can bebranched or linear.

One class of suitable benzenepolycarboxylic acids or a derivativesthereof are the alkyl terephthalates such as monomethyl terephthalate,dimethyl terephthalate, diethyl terephthalate, di-n-propylterephthalate, di-n-butyl terephthalate, di-tert-butyl terephthalate,diisobutyl terephthalate, monoglycol esters of terephthalic acid,diglycol esters of terephthalic acid, di-n-octyl terephthalate,diisooctyl terephthalate, mono-2-ethylhexyl terephthalate,di-2-ethylhexyl terephthalate, di-n-nonyl terephthalate, diisononylterephthalate, di-n-decyl terephthalate, di-n-undecyl terephthalate,diisodecyl terephthalate, diisoundecyl terephthalate, diisododecylterephthalate, di-n-octadecyl terephthalate, diisooctadecylterephthalate, di-n-eicosyl terephthalate, ditridecyl terephthalate,diisotridecyl terephthalate, monocyclohexyl terephthalate and ordicyclohexyl terephthalate. Also suitable are derivates in which thealkyl groups of the ester groups are different alkyl groups. Mixtures ofone or more alkyl terephthalates may be used

Another suitable class are the alkyl phthalates such as monomethylphthalate, dimethyl phthalate, diethyl phthalate, di-n-propyl phthalate,di-n-butyl phthalate, di-tert-butyl phthalate, diisobutyl phthalate,monoglycol esters of phthalic acid, diglycol esters of phthalic acid,di-n-octyl phthalate, diisooctyl phthalate, di-2-ethylhexyl phthalate,di-n-nonyl phthalate, diisononyl phthalate, di-n-decyl phthalate,diisodecyl phthalate, di-n-undecyl phthalate, di-isoundecyl phthalate,diisododecyl phthalate, di-n-octadecyl phthalate, diisooctadecylphthalate, di-n-eicosyl phthalate, monocyclohexyl phthalate,dicyclohexyl phthalate; alkyl isophthalates such as monomethylisophthalate, dimethyl isophthalate, diethyl isophthalate, di-n-propylisophthalate, di-n-butyl isophthalate, di-tert-butyl isophthalate,diisobutyl isophthalate, monoglycol esters of isophthalic acid, diglycolesters of isophthalic acid, di-n-octyl isophthalate, diisooctylisophthalate, di-2-ethylhexyl isophthalate, di-n-nonyl isophthalate,diisononyl isophthalate, di-n-decyl isophthalate, diisodecylisophthalate, di-n-undecyl isophthalate, di-isoundecyl isophthalate,diisododecyl isophthalate, di-n-octadecyl isophthalate, diisooctadecylisophthalate, di-n-eicosyl isophthalate, monocyclohexyl isophthalate andor dicyclohexyl isophthalate. Also suitable are derivates in which thealkyl groups of the ester groups are different alkyl groups. Mixtures ofone or more alkyl phthalates or isophthalates may be used.

A further suitable class are the alkyl trimellitates such as monomethyltrimellitate, dimethyl trimellitate, diethyl trimellitate, di-n-propyltrimellitate, di-n-butyl trimellitate, di-tert-butyl trimellitate,diisobutyl trimellitate, the monoglycol ester of trimellitic acid,diglycol esters of trimellitic acid, di-n-octyl trimellitate, diisooctyltrimellitate, di-2-ethylhexyl trimellitate, di-n-nonyl trimellitate,diisononyl trimellitate, di-n-decyl trimellitate, diisodecyltrimellitate, di-n-undecyl trimellitate, di-isoundecyl trimellitate,diisododecyl trimellitate, di-n-octadecyl trimellitate, diisooctadecyltrimellitate, di-n-eicosyl trimellitate, monocyclohexyl trimellitate,dicyclohexyl trimellitate and trimethyl trimellitate, triethyltrimellitate, tri-n-propyl trimellitate, tri-n-butyl trimellitate,tri-tert-butyl trimellitate, triisobutyl trimellitate, triglycol estersof trimellitic acid, tri-n-octyl trimellitate, triisooctyl trimellitate,tri-2-ethylhexyl trimellitate, tri-n-nonyl trimellitate, tri-isononyltrimellitate, tri-n-decyl trimellitate, triisododecyl trimellitate,tri-n-undecyl trimellitate, tri-isoundecyl trimellitate, triisododecyltrimellitate, tri-n-octadecyl trimellitate, triisooctadecyltrimellitate, tri-n-eicosyl trimellitate and tricyclohexyl trimellitate.Also suitable are derivates in which the alkyl groups of the estergroups are different alkyl groups. Mixtures of one or more alkyltrimellitates may be used.

Also suitable are the alkyl trimesates such as monomethyl trimesate,dimethyl trimesate, diethyl trimesate, di-n-propyl trimesate, di-n-butyltrimesate, di-tert-butyl trimesate, diisobutyl trimesate, monoglycolesters of trimesic acid, diglycol esters of trimesic acid, di-n-octyltrimesate, diisooctyl trimesate, di-2-ethylhexyl trimesate, di-n-nonyltrimesate, diisononyl trimesate, di-n-decyl trimesate, diisodecyltrimesate, di-n-undecyl trimesate, di-isoundecyl trimesate, diisododecyltrimesate, di-n-octadecyl trimesate, diisooctadecyl trimesate,di-n-eicosyl trimesate, monocyclohexyl trimesate, dicyclohexyltrimesate, and also trimethyl trimesate, triethyl trimesate,tri-n-propyl trimesate, tri-n-butyl trimesate, tri-tert-butyl trimesate,triisobutyl trimesate, triglycol esters of trimesic acid, tri-n-octyltrimesate, triisooctyl trimesate, tri-2-ethyl-hexyl trimesate,tri-n-nonyl trimesate, tri-isononyl trimesate, tri-n-decyl trimesate,triisododecyl trimesate, tri-n-undecyl trimesate, tri-isoundecyltrimesate, triisododecyl trimesate, tri-n-octadecyl trimesate,triisooctadecyl trimesate, tri-n-eicosyl trimesate and tricyclohexyltrimesate. Also suitable are derivates in which the alkyl groups of theester groups are different alkyl groups. Mixtures of one or more alkyltrimesates may be used.

A further suitable class are the alkyl hemimellitates such as monomethylhemimellitate, dimethyl hemimellitate, diethyl hemimellitate,di-n-propyl hemimellitate, di-n-butyl hemimellitate, di-tert-butylhemimellitate, diisobutyl hemimellitate, monoglycol esters ofhemimellitic acid, diglycol esters of hemimellitic acid, di-n-octylhemimellitate, diisooctyl hemimellitate, di-2-ethylhexyl hemimellitate,di-n-nonyl hemimellitate, diisononyl hemimellitate, di-n-decylhemimellitate, diisodecyl hemimellitate, di-n-undecyl hemimellitate,di-isoundecyl hemimellitate, diisododecyl hemimellitate, di-n-octadecylhemimellitate, diisooctadecyl hemimellitate, di-n-eicosyl hemimellitate,monocyclohexyl hemimellitate, dicyclohexyl hemimellitate, and alsotrimethyl hemimellitate, triethyl hemimellitate, tri-n-propylhemimellitate, tri-n-butyl hemimellitate, tri-tert-butyl hemimellitate,triisobutyl hemimellitate, triglycol esters of hemimellitic acid,tri-n-octyl hemimellitate, triisooctyl hemimellitate, tri-2-ethylhexylhemimellitate, tri-n-nonyl hemimellitate, tri-isononyl hemimellitate,tri-n-decyl hemimellitate, triisodecyl hemimellitate, tri-n-undecylhemimellitate, tri-isoundecyl hemimellitate, triisododecylhemimellitate, tri-n-octadecyl hemimellitate, triisooctadecylhemimellitate, tri-n-eicosyl hemimellitate and tricyclohexylhemimellitate. Also suitable are derivates in which the alkyl groups ofthe ester groups are different alkyl groups. Mixtures of one or morealkyl hemimellitates may be used.

Another suitable class are the alkyl pyromellitates such as monomethylpyromellitate, dimethylpyromellitate, diethyl pyromellitate, di-n-propylpyromellitate, di-n-butyl pyromellitate, di-tert-butyl pyromellitate,diisobutyl pyromellitate, monoglycol esters of pyromellitic acid,diglycol esters of pyromellitic acid, di-n-octyl pyromellitate,diisooctyl pyromellitate, di-2-ethylhexyl pyromellitate, di-n-nonylpyromellitate, diisononyl pyromellitate, di-n-decyl pyromellitate,diisodecyl pyromellitate, di-n-undecyl pyromellitate, di-isoundecylpyromellitate, diisododecyl pyromellitate, di-n-octadecyl pyromellitate,diisooctadecyl pyromellitate, di-n-eicosyl pyromellitate, monocyclohexylpyromellitate, trimethyl pyromellitate, triethyl pyromellitate,tri-n-propyl pyromellitate, tri-n-butyl pyromellitate, tri-tert-butylpyromellitate, triisobutyl pyromellitate, triglycol esters ofpyromellitic acid, tri-n-octyl pyromellitate, triisooctyl pyromellitate,tri-2-ethylhexyl pyromellitate, tri-n-nonyl pyromellitate, tri-isononylpyromellitate, triisodecyl pyromellitate, tri-n-decyl pyromellitate,tri-n-undecyl pyromellitate, tri-isoundecyl pyromellitate, trisododecylpyromellitate, tri-n-octadecyl pyromellitate, triisooctadecylpyromellitate, tri-n-eicosyl pyromellitate, tricyclohexyl pyromellitate,and also tetramethylpyromellitate, tetraethyl pyromellitate,tetra-n-propyl pyromellitate, tetra-n-butyl pyromellitate,tetra-tert-butyl pyromellitate, tetraisobutyl pyromellitate, tetraglycolesters of pyromellitic acid, tetra-n-octyl pyromellitate, tetraisooctylpyromellitate, tetra-2-ethylhexyl pyromellitate, tetra-n-nonylpyromellitate, tetraisododecyl pyromellitate, tetra-n-undecylpyromellitate, tetraisododecyl pyromellitate, tetra-n-octadecylpyromellitate, tetraisooctadecyl pyromellitate, tetra-n-eicosylpyromellitate, tetracyclohexyl pyromellitate. Also suitable arederivates in which the alkyl groups of the ester groups are differentalkyl groups. Mixtures of one or more alkyl pyromellitates may be used.

Also suitable are anhydrides of phthalic acid, trimellitic acid,hemimellitic acid and pyromellitic acid.

Also suitable are alkyl terephthalates, alkyl phthalates, alkylisophthalates, dialkyl or trialkyl trimellitates, dialkyl or trialkyltrimesates, dialkyl or trialkyl hemimellitates and dialkyl, trialkyl ortetraalkyl pyromellitates in which one or more of the alkyl groupscontain 5, 6 or 7 carbon atoms (e.g. are C₅, C₆ or C₇ alkyl groups) suchalkyl groups include; n-pentyl, 1-methylbutyl terephthalate,2-methylbutyl, 3-methylbutyl, 2,2-dimethylpropyl, 1,1-dimethylpropyl,n-hexyl, 1-methylpentyl, 2-methylpentyl, 3-methylpentyl, 4-methylpentyl,1,1-dimethylbutyl, 2,2-dimethylbutyl, 3,3-dimethylbutyl,1,2-dimethylbutyl, 1,3-dimethylbutyl, 2,3-dimethylbutyl,1-methyl-2-ethylpropyl, 1-ethyl-2-methylpropyl, 1-ethylbutyl,2-ethylbutyl, n-heptyl, 1-methylhexyl, 2-methylhexyl, 3-methylhexyl,4-methylhexyl, 5-methylhexyl, 1,1-dimethylpentyl, 2,2-dimethylpentyl,3,3-dimethylpentyl, 4,4-dimethylpentyl, 1-ethylpentyl, 2-ethylpentyl,3-ethylpentyl, 1,1,2-trimethylbutyl, 1,1,3-trimethylbutyl,1,2,2-trimethylbutyl, 2,2,3-trimethylbutyl, 1,3,3-trimethylbutyl,2,3,3-trimethylbutyl, 1,2,3-trimethylbutyl, 1-ethyl-2-methylbutyl,1-ethyl-3-methylbutyl, 2-ethyl-3-methylbutyl and 1-methyl-2-ethylbutyl.Also envisaged as suitable are compounds in which the alkyl groups arenot identical such as for example in butylpropyl terephthalate or whereone of the alkyl groups is replaced by a benzyl group such as forexample in butylbenzyl terephthalate. Also suitable are mixtures of oneor more alkyl terephthalates, alkyl phthalates, alkyl isophthalates,dialkyl or trialkyl trimellitates, dialkyl or trialkyl trimesates,dialkyl or trialkyl hemimellitates and dialkyl, trialkyl or tetraalkylpyromellitates in which one or more of the alkyl groups contain 5, 6 or7 carbon atoms.

In the process of the present invention it is also possible to usemixtures of one or more of the benzenepolycarboxylic acid or aderivative thereof described herein. When the derivatives are esters themixture may be derived through use of a two or more alcohols inadmixture or in sequence to esterify the same sample of abenzenepolycarboxylic acid derivative or a mixture of two or morebenzenepolycarboxylic acids or a derivatives. Alternatively the alcoholsmay be used to form, in separate syntheses, two different esterifiedderivatives, which may then be mixed together to form a mixture of twoor more esterified derivatives. In either approach the mixture maycomprise a mixture of esters derived from branched or linear alcohols,for example the mixture may comprise ester derivatives prepared from C7,C9, C8, C10 and C11 linear or branched alcohols, preferably linearalcohols, with the alcohols being used in the same synthesis of amixture of derivatives or in separate syntheses of the derivative wherethe resultant derivative products in each synthesis are combined to forma mixed derivative.

In the process of the present invention the preferred products are thosederived from phthalates and in particular the following:cyclohexane-1,2-dicarboxylic acid di(isopentyl) ester, obtainable byhydrogenation of a di(isopentyl) phthalate having the Chemical Abstractsregistry number (in the following: CAS No.) 84777-06-0;cyclohexane-1,2-dicarboxylic acid di(isoheptyl) ester, obtainable byhydrogenating the di(isoheptyl) phthalate having the CAS No. 71888-89-6;cyclohexane-1,2-dicarboxylic acid di(isononyl) ester, obtainable byhydrogenating the di(isononyl)phthalate having the CAS No. 68515-48-0;cyclohexane-1,2-dicarboxylic acid di(isononyl) ester, obtainable byhydrogenating the di(isononyl)phthalate having the CAS No. 28553-12-0,which is based on n-butene; cyclohexane-1,2-dicarboxylic aciddi(isononyl) ester, obtainable by hydrogenating thedi(isononyl)phthalate having the CAS No. 28553-12-0, which is based onisobutene; a 1,2-di-C₉-ester of cyclohexanedicarboxylic acid, obtainableby hydrogenating the di(nonyl)phthalate having the CAS No. 68515-46-8;cyclohexane-1,2-dicarboxylic acid di(isodecyl) ester, obtainable byhydrogenating a di(isodecyl)phthalate having the CAS No. 68515-49-1;1,2-C₇₋₁₁-ester of cyclohexanedicarboxylic acid, obtainable byhydrogenating the corresponding phthalic acid ester having the CAS No.68515-42-4; 1,2-di-C₇₋₁₁-ester of cyclohexanedicarboxylic acid,obtainable by hydrogenating the di-C₇₋₁₁-phthalates having the followingCAS Nos.: 111381-89-6, 111381-90-9, 111381-91-0, 68515-44-6, 68515-45-7and 3648-20-7; a 1,2-di-C₉₋₁₁-ester of cyclohexanedicarboxylic acid,obtainable by hydrogenating a di-C₉₋₁₁-phthalate having the CAS No.98515-43-5; a 1,2-di(isodecyl)cyclohexanedicarboxylic acid ester,obtainable by hydrogenating a di(isodecyl)phthalate, consistingessentially of di-(2-propylheptyl)phthalate;1,2-di-C₇₋₉-cyclohexanedicarboxylic acid ester, obtainable byhydrogenating the corresponding phthalic acid ester, which comprisesbranched and linear C₇₋₉-alkylester groups; respective phthalic acidesters which may be e.g. used as starting materials have the followingCAS Nos.: di-C₇₋₉-alkylphthalate having the CAS No. 111 381-89-6;di-C₇₋₉-alkylphthalate having the CAS No. 68515-44-6; anddi-C₉-alkylphthalate having the CAS No. 68515-45-7.

More preferably, the above explicitly mentioned C₅₋₇, C₉, C₁₀, C₇₋₁₁,C₉₋₁₁ and C₇₋₉ esters of 1,2-cyclohexanedicarboxylic acids arepreferably the hydrogenation products of the commercially availablebenzenepolycarboxylic acid esters with the trade names Jayflex® DINP(CAS No. 68515-48-0), Jayflex® DIDP (CAS No. 68515-49-1), Jayflex® DIUP(CAS No. 85507-79-5), Jayflex® DTDP (CAS No. 68515-47-9), Palatinol®911P, Vestinol® 9 (CAS No. 28553-12-0), TOTM-I® (CAS No. 3319-31-1),Linplast® 68-TM and Palatinol® N (CAS No. 28553-12-0) which are used asplasticizers in plastics.

Further examples of commercially available benzenepolycarboxylic acidesters suitable for use in the present invention include phthalates suchas: Palatinol® AH (Di-(2-ethylhexyl) phthalate; Palatinol® AH L(Di-(2-ethylhexyl) phthalate); Palatinol® C (Dibutyl phthalate);Palatinol® IC (Diisobutyl phthalate); Palatinol® N (Diisononylphthalate); Palatinol® Z (Diisodecyl phthalate) Palatinol® 10-P(Di-(2-Propylheptyl) phthalate); Palatinol® 711P (Heptylundecylphthalate); Palatinol® 911 (Nonylundecyl phthalate); Palatinol® 11P-E(Diundecyl phthalate); Palatinol® M (Dimethyl phthalate); Palatinol® A(Diethyl phthalate); Palatinol® A (R) (Diethyl phthalate); andPalatinol® K (Dibutylglycol phthalate). Further examples are thecommercially available adipates such as: Plastomoll® DOA(Di-(2-ethylhexyl) adipate) and Plastomoll® DNA (Diisononyl adipate).Further examples of suitable commercially available materials areVestinol® C (DBP), Vestinol® IB (DIBP), Vestinol® AH (DEHP), Witamol®110 (610P) and Witamol® 118 (810P).

For the purposes of the present invention, the terms “macropores” and“mesopores” are used as they are defined in Pure Appl. Chem., 45 (1976),79, namely as pores whose diameter is above 50 nm (macropores) or whosediameter is from 2 nm and 50 nm (mesopores).

The catalyst may be prepared using a wide variety of porous andnon-porous support materials that are well known in the art. Theseinclude but are not limited to alumina, silica, TiO₂, ZrO₂, activatedcarbon, silicon carbide, magnesium oxide, zinc oxide and similarinorganic oxides or mixtures of two or more thereof. The preferredsupport materials are alumina, silica or mixtures thereof, with the mostpreferred material being silica, especially amorphous silica. In theprocess of the present invention the support is preferably a poroussupport. In one embodiment the support is preferably a support thatcomprises mesopores and most preferably as support that is substantiallycompletely mesoporous or has as a major component, when the support is amixture of two or more materials, at least one material that issubstantially completely mesoporous. The preferred materials for use assupports in the present invention are amorphous materials such asalumina and silica with the most preferred support being amorphoussilica. A further class of materials that may be used as supports in thepresent invention are crystalline materials such as crystallinemolecular sieve materials and more preferably crystalline molecularsieve materials that are mesoporous. A further class of materials thatmay be use are ordered mesoporous materials.

Ordered mesoporous molecular sieve materials, which may be used assupports in the present invention, are those materials that may besynthesized using amphiphilic compounds as directing agents. Examples ofsuch materials are described in U.S. Pat. No. 5,250,282, the wholecontents of which are hereby incorporated by reference. Examples ofamphiphilic compounds are also provided in Winsor, Chemical Reviews,68(1), 1968. Other suitable ordered mesoporous materials of this typeare also described in “Review of Ordered Mesoporous Materials”, U.Ciesla and F. Schuth, Microporous and Mesoporous Materials, 27, (1999),131-49. Such materials include but are not limited to materialsdesignated as SBA (Santa Barbara) such as SBA-2, SBA-15 and SBA-16,materials designated as FSM (Folding Sheet Mechanism) such as FSM-16 andKSW-2, materials designated as MSU (Michigan State) such as MSU-S andMSU-X, materials designated as TMS or Transition Metal Sieves, materialsdesignated as FMMS or functionalized monolayers on mesoporous supportsand materials designated as APM or Acid Prepared Mesostructure.Particularly preferred ordered mesoporous materials are the silicate oraluminosilicate ordered mesoporous materials designated as M41S such asMCM-14, MCM-22, MCM-41, MCM-48, MCM-49, and MCM-50. These orderedmesoporous materials are described in detail in U.S. Pat. No. 5,102,643,the whole contents of which are hereby incorporated by reference. Aparticularly suitable sub-class of this family of materials for use inthe present invention are the mesoporous silicas designated as MCM-41and MCM-48. MCM-41 is particularly preferred and has a hexagonalarrangement of uniformly sized mesopores. MCM-41 molecular sievematerials are described in detail in U.S. Pat. No. 5,098,684, the wholecontents of which are hereby incorporated by reference. The MCM-41molecular sieves generally have a SiO₂/Al₂O₃ molar ratio when alumina ispresent and it is preferred that the SiO₂/Al₂O₃ molar ratio for thesematerials is greater than 100, preferably greater than 200, and mostpreferably greater than 300.

In one embodiment of the present invention, the hydrogenation processutilizes a catalyst, which comprises a hydrogenation function in theform of at least one active metal site on a support material comprisingone or more ordered mesoporous materials with a unique structure andpore geometry as described below. These materials are inorganic, porous,non-layered materials which, in their calcined forms exhibit an X-raydiffraction pattern with at least one peak at a d-spacing greater thanabout 18 Angstrom Units (Å). They also have a benzene adsorptioncapacity of greater than 15 grams of benzene per 100 grams of thematerial at 50 torr and 25° C. In a preferred form, the support materialis characterized by a substantially uniform hexagonal honeycombmicrostructure with uniform pores having a cell diameter greater than 2nm and typically in the range of 2 to 50 nm, more preferably 5 to 20 nm,and most preferably from 3 to 20 nm. Most prominent among thesematerials is a material identified as MCM-41, which is usuallysynthesized as a metallosilicate with Broensted acid sites byincorporating a tetrahedrally coordinated trivalent element such as Al,Ga, B, or Fe within the silicate framework. The preferred forms of thesematerials are the aluminosilicates although other metallosilicates mayalso be utilized. MCM-41 is characterized by a microstructure with auniform, hexagonal arrangement of pores with diameters of at least about2 nm: after calcination it exhibits an X-ray diffraction pattern with atleast one d-spacing greater than about 18 Å and a hexagonal electrondiffraction pattern that can be indexed with a d₁₀₀ value of greaterthan about 18 Å, which corresponds to the d-spacing of the peak in theX-ray diffraction pattern. This material is described below and indetail in Ser. No. 07/625,245, now U.S. Pat. No. 5,098,684 (Kresge etal) and U.S. Pat. No. 5,102,643 to Kresge et al., both of which areincorporated herein in their entirety.

The ordered mesoporous materials may be crystalline, that is havingsufficient order to provide a diffraction pattern such as, for example,by X-ray, electron or neutron diffraction, following calcination, withat least one peak. These mesoporous materials may be characterized bytheir structure, which includes extremely large pore windows as well ashigh sorption capacities.

Ordered mesoporous materials as used in the present invention can bedistinguished from other porous inorganic solids by the regularity oftheir large open pores, whose pore size more nearly resembles that ofamorphous or paracrystalline materials, but whose regular arrangementand uniformity of size (pore size distribution within a single phase of,for example, +/−25%, usually +/−15% or less of the average pore size ofthat phase) resemble more those of crystalline framework materials suchas zeolites. The term “hexagonal” is intended to encompass not onlymaterials that exhibit mathematically perfect hexagonal symmetry withinthe limits of experimental measurement, but also those with significantobservable deviations from that ideal state. A working definition asapplied to the microstructure of the present invention would be thatmost channels in the material would be surrounded by six nearestneighbor channels at roughly the same distance. Defects andimperfections will cause significant numbers of channels to violate thiscriterion to varying degrees, depending on the quality of the material'spreparation. Samples which exhibit as much as +/−25% random deviationfrom the average repeat distance between adjacent channels still clearlygive recognizable images of the present ordered mesoporous materials.

The ordered mesoporous materials as used for preparation of the catalystsupport preferably have the following composition:M_(n/q)(W_(a)X_(b)Y_(c)Z_(d)O_(h))

wherein W is a divalent element, such as a divalent first row transitionmetal, e.g. manganese, cobalt and iron, and/or magnesium, preferablycobalt; X is a trivalent element, such as aluminium, boron, iron and/orgallium, preferably aluminium; Y is a tetravalent element such assilicon and/or germanium, preferably silicon; Z is a pentavalentelement, such as phosphorus; M is one or more ions, such as, forexample, ammonium, Group IA, IIA and VIIB ions, usually hydrogen, sodiumand/or fluoride ions; n is the charge of the composition excluding Mexpressed as oxides; q is the weighted molar 1 average valence of M; n/qis the number of moles or mole fraction of M; a, b, c, and d are molefractions of W, X, Y and 1 Z, respectively; h is a number of from 1 to2.5; and (a+b+c+d)=1. A preferred embodiment of the above crystallinematerial is when (a+b+c) is greater than d, and h=2. A furtherembodiment is when a and d=0, and h=2. In the as-synthesised form, themesoporous material has a composition, on an anhydrous basis, expressedempirically as follows:rRM_(n/q)(W_(a)X_(b)Y_(c)Z_(d)O_(h))

wherein R is the total organic material not included in M as an ion, andr is the coefficient for R, i.e. the number of moles or mole fraction ofR. The M and R components are associated with the material as a resultof their presence during crystallisation, and are easily removed or, inthe case of M, replaced by post-crystallisation methods hereinafter moreparticularly described.

To the extent desired, the original M, e.g. ammonium, sodium orchloride, ions of the as-synthesised material can be replaced inaccordance with techniques well known in the art, at least in part, byion exchange with other ions. Preferred replacing ions include metalions, hydrogen ions, hydrogen precursor, e.g. ammonium, ions andmixtures thereof. Other M ions include rare earth metals and metals ofGroups IA (e.g. K), IIA (e.g. Ca), VIIA (e.g. Mn), VIIA (e.g. Ni), IB(e.g. Cu), IIB (e.g. Zn), IIIB (e.g. In), IVB (e.g. Sn), and VIIB (e.g.F) of the Periodic Table of the Elements (Sargent-Welch Co. Cat. No.S-18806, 1979) and mixtures thereof.

The preferred support for use in the present invention is a silicasupport. The preferred ordered mesoporous materials for use in theprocess of the present invention are the ordered mesoporous silicas. Themost preferred ordered mesoporous silicas are those designated as M41S,with the most preferred being MCM-41.

Further examples of a mesoporous materials that may be used in theprocess of the present invention are the mesoporous silicas as describedin and prepared according to U.S. Pat. No. 5,951,962, the disclosure ofwhich is incorporated herein in its entirety. In this referencemesoporous silica is prepared by converting a silica precursor in awater and polymer dispersion containing reaction medium. The preferredpolymer dispersion is a cationic polymer.

High surface area mesoporous alumina solids may be used in preparing thecatalyst supports for use in the process of the present invention; suchhigh surface area mesoporous alumina solids may be prepared according tothe methods described in U.S. Pat. No. 6,238,701, the disclosure ofwhich is incorporated herein in its entirety.

In one embodiment the support may be macroporous materials or materialsthat are both macroporous and mesoporous, such as those described inU.S. Pat. Nos. 5,936,126, 6,248,924 and 6,284,917 the disclosures ofwhich are incorporated herein in their entirety.

Such macroporous materials have a mean pore diameter of at least about50 nm, preferably at least about 100 nm, in particular at least about500 nm. Preferably these macroporous materials have a BET surface areathat is at most about 30 m²/g, preferably at most about 15 m²/g, morepreferably at most about 10 m²/g in particular at most about 5 m²/g andmore preferably at most about 3 m²/g. The mean pore diameter of thesesmacroporous materials is preferably from about 100 nm to about 20000 nm,and more preferably from about 500 nm to about 5000 nm, and mostpreferably 500 nm to 1000 nm. The surface area of these macroporousmaterials is preferably from about 0.2 to about 15 m²/g, more preferablyfrom about 0.5 to about 10 m²/g, in particular from about 0.5 to about 5m²/g and more preferably from about 0.5 to about 3 m²/g. In thisembodiment the pore size distribution of the macroporous material ispreferably approximately bimodal, with the pore diameter distributionhaving one maxima at about 600 nm. Further preference is given to amacroporous material, which has a surface area of 1.75 m²/g and thisbimodal distribution of the pore diameter. The pore volume of thepreferred macroporous material is preferably about 0.53 ml/g.

In a further embodiment the one or more materials of mixed porosity maybe used in addition to a silica support and/or one or more materialshaving mesopores. These materials of mixed porosity may possessmesopores in addition to their macropores. Examples of such material aredescribed in U.S. Pat. Nos. 6,248,924 and 6,284,917, the disclosures ofwhich are incorporated herein in their entirety. In this embodiment thematerials of mixed porosity may have a pore distribution in which fromabout 5 to about 50%, preferably from about 10 to about 45%, morepreferably from about 10 to about 30% and in particular from about 15 toabout 25%, of the pore volume is formed by macropores having porediameters in the range from about 50 nm to about 10,000 nm and fromabout 50 to about 95%, preferably from about 55 to about 90%, morepreferably from about 70 to about 90% and in particular from about 75 toabout 85%, of the pore volume is formed by mesopores having a porediameter of from about 2 to about 50 nm where in each case the sum ofthe pore volumes adds up to 100%.

In this embodiment the total pore volume of the mixed porosity materialis from about 0.05 to 1.5 cm³/g, preferably from 0.1 to 1.2 cm³/g and inparticular from about 0.3 to 1.0 cm³/g. The mean pore diameter of themixed porosity material is preferably from about 5 to 20 μm, preferablyfrom about 8 to about 15 nm and in particular from about 9 to about 12nm.

The surface area of the mixed porosity material is preferably from about50 to about 600 m²/g, more preferably from about 200 to about 600 m²/gand in particular from about 250 to about 600 m²/g of the support.

The surface area of the macroporous materials and mixed porositymaterials may be determined by the BET method using N₂ adsorption, inparticular in accordance with DIN 66131. The mean pore diameter and thesize distribution may be determined by Hg porosimetry, in particular inaccordance with DIN 66133.

The macroporous materials and mixed porosity materials that may be usedare, for example, macropore containing activated carbon, siliconcarbide, aluminum oxide, silicon dioxide, titanium dioxide, zirconiumdioxide, magnesium oxide, zinc oxide or mixtures of two or more thereof,with preference being given to using macropore containing alumina.

In one embodiment of the present invention the catalyst may consistsolely of one or more active hydrogenation metals deposited on thesurfaces of one or more supports such as amorphous silica or orderedmesoporous materials. In this embodiment the catalyst is free of addedinorganic binder. The support with or without active metal depositedthereon may be shaped into a wide variety of particle sizes. Generallyspeaking, the particles can be in the form of a powder, a granule, or amolded product, such as an extrudate having particle size sufficient topass through a 2 mesh (Tyler) screen and be retained on a 400 mesh(Tyler) screen. In cases where the catalyst is molded, such as byextrusion, the crystals can be extruded before drying or partially driedand then extruded.

In a further embodiment the support material may be formed intocomposites with matrix materials resistant to the temperatures and otherconditions employed in the hydrogenation process. Such materials includeactive and inactive materials and synthetic or naturally occurringzeolites as well as inorganic materials such as clays and/or oxides suchas alumina, silica or silica-alumina The latter may be either naturallyoccurring or in the form of gelatinous precipitates or gels includingmixtures of silica and metal oxides. Use of a material in conjunctionwith the zeolite, i.e., combined therewith or present during itssynthesis, which itself is catalytically active may change theconversion and/or selectivity of the catalyst. These materials may beincorporated into naturally occurring clays, e.g., bentonite and kaolin,to improve the crush strength of the catalyst under commercial operatingconditions and function as binders or matrices for the catalyst. Thecatalyst support may be composited with the matrix material in amountsfrom 99:01 to 05:95 by weight, preferably from 99:01 to 10:90, morepreferably from 99:01 to 20:80, and most preferably from 99:01 to 50:50catalyst support:matrix material. Preferably, if used the additionalmatrix material is kept to a minimum typically less than 50 wt % of thecombined weight of catalyst support and matrix material, ideally lessthan 40 wt %, preferably less than 30 wt %, more preferably less than 20wt %, more preferably less than 15 wt %, most preferably less than 10 wt% and in a most preferred embodiment less than 5 wt %. Formation of thecomposition may be achieved by conventional means including mulling thematerials together followed by extrusion of pelletizing into the desiredfinished catalyst particles. Ideally the additional matrix material ismacroporous or is a material of mixed porosity i.e. both macroporous andmesoporous. The materials of mixed porosity may have a pore distributionin which from about 5 to about 50%, preferably from about 10 to about45%, more preferably from about 10 to about 30 and in particular fromabout 15 to about 25%, of the pore volume is formed by macropores havingpore diameters in the range from about 50 nm to about 10,000 nm and fromabout 50 to about 95%, preferably from about 55 to about 90%, morepreferably from about 70 to about 90% and in particular from about 75 toabout 85%, of the pore volume is formed by mesopores having a porediameter of from about 2 to about 50 nm where in each case the sum ofthe pore volumes adds up to 100%.

When used, the total pore volume of the mixed porosity material is fromabout 0.05 to 1.5 cm³/g, preferably from 0.1 to 1.2 cm³/g and inparticular from about 0.3 to 1.0 cm³/g. The mean pore diameter of themixed porosity material is preferably from about 5 to 20 nm, preferablyfrom about 8 to about 15 nm and in particular from about 9 to about 12nm. The surface area of the mixed porosity material is preferably fromabout 50 to about 500 m²/g, more preferably from about 200 to about 350m²/g and in particular from about 250 to about 300 m²/g of the support.

The surface area of the macroporous materials and mixed porositymaterials may be determined by the BET method using N₂ adsorption, inparticular in accordance with DIN 66131. The mean pore diameter and thesize distribution may be determined by Hg porosimetry, in particular inaccordance with DIN 66133.

The macroporous materials and mixed porosity materials that may be usedare, for example, macropore containing activated carbon, siliconcarbide, aluminum oxide, silicon dioxide, titanium dioxide, zirconiumdioxide, magnesium oxide, zinc oxide or mixtures of two or more thereof,with preference being given to using macropore containing alumina

The catalyst used in the present invention comprises one or more activehydrogenation metals deposited on one or more support materials. Thehydrogenation component is provided by a metal or combination of metals.Active metals that may be used are preferably one or more metals oftransition group VIII of the Periodic Table. Preference is given tousing platinum, rhodium, palladium, cobalt, nickel or ruthenium or amixture of two or more thereof as active metal. A particular preferenceis given to using ruthenium, platinum, palladium nickel or mixtures oftwo or more thereof. A particularly preferred active metal is rutheniumor nickel, most preferably ruthenium. It has to be noted in this respectthat besides one or more metals of transition group VIII metals othermetals may used be used in combination with the group VIII metals suchas Group IB, VIIB, or VIIIB metals.

The content of the metal component will vary according to its catalyticactivity. Thus, the highly active noble metals may be used in smalleramounts than the less active base metals. For example, about 1 wt.percent or less or ruthenium, palladium or platinum will be effective.The metal component may exceed about 30 percent in a monolayer.

The active metal content is generally from about 0.01 to about 30% byweight, preferably from about 0.01 to about 5% by weight and inparticular from about 0.1 to about 5% by weight, in each case based onthe total weight of the catalyst used. A preferred catalyst is one thatcomprises ruthenium alone or in combination with one or more additionalactive metals at a total content of less than 5% by weight of activemetal and preferably at a total content of less than 2% by weight ofactive metal. Preferably the content of ruthenium is from about 0.01 to2%, more preferably 0.1 to 1% by weight of the total catalyst. When thesupport is used in combination with a matrix material it is preferredthat the catalytically active metal sites are formed on the supportbefore it is combined with the matrix material.

The hydrogenation catalyst is manufactured using a process according tothe present invention in which a support is provided with one or morecatalytically active metal sites through the use of a specific sequenceof process steps. In the first step the support is provided with one ormore organic complexes of one or more catalytically active metals in asecond step the organic complex is either fully or partially decomposed.

In one embodiment a compound, or salt, of one or more catalyticallyactive metals is combined with one or more organic compounds to form amixture which is then contacted with a support to deposit the organiccomplex. In this embodiment the complex may be formed on formation ofthe mixture or may be formed after contact with the support and afterremoval of any solvent or solvents used during formation of the mixture.In another embodiment the support is first contacted with a compound, orsalt, of one or more catalytically active metals followed by treatmentwith one or more organic compounds to form the organic complex on thesupport. In an alternative embodiment the support is first contactedwith one or more organic compounds followed by treatment with acompound, or salt, or one or more catalytically active metals to formthe complex on the support. In a further embodiment one or more organiccompounds and a compound, or salt, or one or more catalytically activemetals are contacted simultaneously with the support to form the organiccomplex. In yet a further embodiment a suitable organic complex of thedesired metal may be synthesised and applied to the support via solutionof the complex in a suitable solvent for the complex.

The one or more catalytically active metals may be exchanged onto thesupport material, impregnated into it or physically admixed with it. Theapplication of the individual components or mixture of components may beachieved by steeping the support in an aqueous metal salt solution, or asolution in a suitable solvent of a compound of the metal, or in themixture. The deposition may be achieved by dipping, spraying or anyother method. Suitable metal salts for preparing the metal saltsolutions are for example nitrates, nitrosyl nitrates, halides,carbonates, carboxylates, acetylacetonates, chloro complexes, nitritocomplexes or amine complexes of the corresponding metals, withpreference being given to the nitrates and nitrosyl nitrates and mostpreferably the nitrosyl nitrates. When Pt is the active metal it ispreferred that it is not complexed with the organic compound as itsnitrate salt, preferably it is complexed as a chloride or hydroxidesalt.

In the case of catalysts, which have a plurality of active metalsapplied to the support, the metal salts or metal salt solutions or metalcompound solutions or mixtures may be applied simultaneously or insuccession.

In the process of the present invention any organic compounds that arecapable of forming organic complexes with the one or more catalyticallyactive metals may be used. Typically these will be organic compoundsthat are capable of forming complexes that are stable under theconditions that are normally used for depositing catalytically activemetals. Ideally, the organic compounds are selected to provide metalorganic complexes that are stable under the conditions normally used fordrying catalyst supports after impregnation with one or morecatalytically active metals. Suitable organic compounds are well knownin the art of transition metal chemistry and include such organiccompounds as organic chelating agents, organic monodentate, bidentateand polydentate ligands commonly used in the preparation of transitionmetal coordination complexes. In a number of such complexes one or moreligands being covalently bonded molecules and/or ions may be present inthe complex.

In the process of the present invention particularly suitable organiccompounds are compounds that contain one or more amino groups such asamines or amino acids and most preferably organic compounds containingamino and alcohol groups.

The compounds containing one or more amino groups may be aliphaticamines, cycloaliphatic amines, aralkyl amines and alkylaryl amines.These may be primary, secondary and tertiary amines. They may also bequaternary ammonium salts with a counter ion. It is preferred that thenitrogen-containing compound is one or more primary, secondary ortertiary amines, preferably one or more aliphatic amines and mostpreferably one or more amines having one or more hydroxyl groups such asfor example hydroxyalkylamines.

In one embodiment, the nitrogen-containing compound used according tothe present invention has the following general formula:NR¹R²R³  (I)

wherein R¹, R² and R³ independently are one or more of the followinggroups: C₁-C₅₀-alkyl, C₃-C₅₀-cycloalkyl, aromatic, alkyl substitutedaromatic, such as C₁-C₅₀-alkyl substituted aromatic, aromaticsubstituted aliphatic moieties such as C₁-C₅₀-alkylene moietiessubstituted with one or more aromatic groups, C₁-C₅₀-hydroxyalkyl,amino- and/or hydroxyl-substituted C₁-C₅₀-alkyl, alkoxyalkyl such asC₂-C₅₀-alkoxyalkyl, dialkylaminoalkyl such as C₃-C₅₀-dialkylaminoalkyl,alkylaminoalkyl such as C₂-C₅₀-alkylaminoalkyl, heterocyclic, aromaticheterocyclic, alkyl substituted heterocyclic and alkyl substitutedaromatic heterocyclic, such as C₁-C₅₀-alkyl substituted heterocyclic andaromatic heterocyclic compounds, and heterocyclic substituted aliphaticmoieties such as C₁-C₅₀-alkylene moieties substituted with one or morearomatic groups. In addition, R¹ and R² may independently be hydrogen.In another embodiment, R¹ and R² may form, with the nitrogen atom, anitrogen-containing heterocycle, aromatic heterocycle, alkyl substitutedheterocycle or alkyl substituted aromatic heterocycle.

Examples of alkyl groups include; methyl, ethyl, n-propyl, isopropyl,n-butyl, isobutyl, sec-butyl, tert-butyl, n-pentyl, isopentyl,sec-pentyl, neopentyl, 1,2-dimethylpropyl, n-hexyl, isohexyl, sec-hexyl,n-heptyl, isoheptyl, n-octyl, isooctyl, 2-ethylhexyl, n-decyl,2-n-propyl-n-heptyl, n-tridecyl, 2-n-butyl-n-nonyl and3-n-butyl-n-nonyl, particularly preferably ethyl, isopropyl,2-ethylhexyl, n-decyl, 2-n-propyl-n-heptyl, n-tridecyl,2-n-butyl-n-nonyl and 3-n-butyl-n-nonyl, and C₄₀-C₂₀₀-alkyl such aspolybutyl, polyisobutyl, polypropyl, polyisopropyl and polyethyl. Themost preferred aliphatic amines are aliphatic amines having one or morealkyl groups having 1 to 20 carbon atoms and more preferably 2 to 14carbon atoms.

Examples of cycloalkyl groups include C₃-C₁₂-cycloalkyl, preferablyC₃-C₈-cycloalkyl such as cyclopropyl, cyclobutyl, cyclopentyl,cyclohexyl, cycloheptyl and cyclooctyl.

Examples of aromatic groups include; phenyl, 1-naphthyl, 2-naphthyl,1-anthryl, 2-anthryl and 9-anthryl, 1-phenanthryl, 2-phenanthryl,3-phenanthryl, 4-phenanthryl and 9-phenanthryl.

Examples of alkyl substituted aromatic groups include C₇-C₅₀ alkylaromatic groups, preferably C₇-C₄₀-alkylphenyl such as 2-nonylphenyl,3-nonlyphenyl, 4-nonylphenyl, 2-decylphenyl, 3-decylphenyl,4-decylphenyl, 2,3-dinonylphenyl, 2,4-dinonylphenyl, 2,5-dinonylphenyl,3,4-dinonylphenyl, 3,5-dinonylphenyl, 2,3-didecylphenyl,2,4-didecylphenyl, 2,5-didecylphenyl, 3,4-didecylphenyl and3,5-didecylphenyl, more preferably C₇-C₁₂ alkylphenyl such as2-methylphenyl, 3-methylphenyl, 4-methylphenyl, 2,4-dimethylphenyl,2,5-dimethylphenyl, 2,6-dimethylphenyl, 3,4-dimethylphenyl,3,5-dimethylphenyl, 2,3,4-trimethylphenyl, 2,3,5-trimethylphenyl,2,3,6-trimethylphenyl, 2,4,6-trimethylphenyl, 2-ethylphenyl,3-ethylphenyl, 4-ethylphenyl, 2-n-propylphenyl, 3-n-propylphenyl and4-n-propylphenyl.

Examples of aromatic substituted aliphatic moieties include C₇-C₅₀alkylene moieties substituted with one or more aromatic substituents,preferably C₇-C₁₂-phenylalkyl such as benzyl, 1-phenethyl, 2-phenethyl,1-phenylpropyl, 2-phenylpropyl, 3-phenylpropyl, 1-phenylbutyl,2-phenylbutyl, 3-phenylbutyl and 4-phenylbutyl, particularly preferablybenzyl, 1-phenethyl and 2-phenethyl.

Examples of hydroxyalkyl groups include C₁-C₅₀-hydroxyalkyl, preferablyC₁-C₈-hydroxyalkyl, particularly preferably C₁-C₄-hydroxyalkyl such ashydroxymethyl, 1-hydroxyethyl, 2-hydroxyethyl, 1-hydroxy-n-propyl,2-hydroxy-n-propyl, 3-hydroxy-n-propyl and 1-hydroxy-methyl-ethyl.Particularly preferred hydoxyalkyl group containing nitrogen compoundsinclude the mono-, di-, and tri-, substituted aliphatichydroxyalkylamines such as methanolamine, di-methanolamine,tri-methanolamine, ethanolamine, di-ethanolamine, tri-ethanolamine,butanolamine, di-butanolamine, tri-butanolamine, propanolamine,di-propanolamine, and tri-propanolamine.

Examples of amino- and hydroxyalkyl groups include C₁-C₅₀-alkyl,preferably amino- and/or hydroxyl-substituted C₁-C₈-alkyl, particularlypreferably amino and/or hydroxyl-substituted C₁-C₄-alkyl such asN-(hydroxyethyl)aminoethyl and N-(aminoethyl)aminoethyl.

Examples of alkoxyalkyl groups include C₂-C₅₀-alkoxyalkyl, preferablyC₂-C₂₀-alkoxyalkyl, particularly preferably C₂-C₈-alkoxyalkyl such asmethoxymethyl, ethoxymethyl, n-propoxymethyl, isopropoxymethyl,n-butoxymethyl, isobutoxymethyl, sec-butoxymethyl, tert-butoxymethyl,1-methoxyethyl and 2-methoxyethyl, particularly preferablyC₂-C₄-alkoxyalkyl such as methoxymethyl, ethoxymethyl, n-propoxymethyl,isopropoxymethyl, n-butoxymethyl, isobutoxymethyl, sec-butoxymethyl,tert-butoxymethyl, 1-methoxyethyl and 2-methoxyethyl.

Examples of dialkylamino groups include C₃-C₅₀-dialkylaminoalkyl,preferably C₃-C₂₀-dialkylaminoalkyl, particularly preferablyC₃-C₁₀-dialkylaminoalkyl such as dimethylaminomethyl,dimethylaminoethyl, diethylaminoethyl, di-n-propylaminoethyl anddiisopropylaminoethyl.

Examples of alkylaminoalkyl groups include C₂-C₅₀-alkylaminoalkyl,preferably C₂-C₂₀-alkylaminoalkyl, particularly preferablyC₂-C₈-alkylaminoalkyl such as methylaminomethyl, methylaminoethyl,ethylaminomethyl, ethylaminoethyl and iso-propylaminoethyl.

Examples of aromatic heterocycles include 2-pyridinyl, 3-pyridinyl,4-pyridinyl, pyrazinyl, 3-pyrrolyl, 2-imidazolyl, 2-furanyl and3-furanyl. Examples of alkyl substituted aromatic heterocycles includeC₄-C₅₀-mono-hetarylalkyl, such as 2-pyridylmethyl, 2-furanyl-methyl,3-pyrrolylmethyl and 2-imidazolylmethyl, and C₄-C₅₀-alkylhetaryl such as2-methyl-3-pyridinyl, 4,5-dimethyl-2-imidazolyl, 3-methyl-2-furanyl and5-methyl-2-pyrazinyl.

Examples of alkylaminoalkyl groups include C₂-C₅₀-alkylaminoalkyl,preferably C₂-C₁₆-alkylaminoalkyl such as methylaminomethyl,methylaminoethyl, ethylaminomethyl, ethylaminoethyl andisopropylaminoethyl.

Examples of dialkylaminoalkyl groups include C₃-C₅₀-dialkylaminoalkyl,preferably C₃-C₁₆-dialkylaminoalkyl such as dimethylaminomethyl,dimethylaminoethyl, diethylaminoethyl, di-n-propylaminoethyl anddiisopropylaminoethyl.

Examples of heterocyclic compounds, include pyridine, pyrrole,imidazole, oxazole, thiazole, pyrazole, 3-pyrroline, pyrrolidine,pyrimidine, and substituted examples of these heterocyclic compounds.Examples of organonitrile compounds include acrylonitrile, alkylnitrites such as for example methyl nitrile, and ethyl nitrile.

Suitable amino acids include natural and synthetic amino acids. Thenatural amino acids include all isomers of the following: alanine,arginine, asparagines, aspartic acid, cysteine, cystine,3,5-dibromotyrosine, 3,5, diiodotyrosine, glutamic acid, glutamine,glycine, histidine, hydroxylysine, hydroxyproline, isoleucine, leucine,lysine, methionine, phenylalanine, proline, serine, threonine,thyroxine, tryptophane, tyrosine and valine, a particularly preferredamino acid is L-arginine.

The organic compound may be used at any suitable level in relation tothe amount of salt or compound of the catalytically active metal.Ideally it is used at an appropriate mole ratio to convert all of thesalt or compound of the catalytically active metal to one or moreorganic complexes. This may be a molar ratio of 1:1 or higher dependingon the capacity of the metal to complex with the organic compound, thecapacity of the organic compound to complex with the metal and thepresence of other complexing ligands such as monodentate ligands.However it is possible to use levels of organic compound which areinsufficient to complex with all of the catalytically active metal; inthese circumstances not all of the metal is converted to organic complexand the resulting catalyst may contain catalytically active metal sitesthat have been derived from complexed and non-complexed metalintermediates. Ideally, the mole ratio of organic compound tocatalytically active metal is within the range of 0.1:1 to 40:1,preferably, 0.1:1 to 30:1, more preferably 0.2:1 to 25:1, even morepreferably 0.25:1 to 10:1 or 0.5:1 to 10:1, more preferably 0.25:1 to5:1, and most preferably 0.5:1 to 5:1.

When the complex is formed in a mixture before contact with the supportthe mixture is usually and preferably formed in combination with asolvent, which may be water or an organic solvent or a mixture of waterand solvent. The amount of solvent used may vary within wide ranges butis typically sufficient to ensure that the mixture may be effectivelycontacted with the support so as to wet support and when the support isporous to allow penetration of the mixture into the porous support.Typically the salt or compound of one or more catalytically activemetals and the organic compound(s) are used in amounts which dependingon their form allow the required mole ratios indicated above to beachieved in the mixture. The remainder of the mixture comprises one ormore solvents which may be present in an amount from 1 to 99 wt % of theweight of the total mixture, preferably 5 to 90 wt % of the weight ofthe total mixture, more preferably 5 to 80 wt % of the weight of thetotal mixture, even more preferably 10 to 70 wt % of the weight of thetotal mixture and most preferably 10 to 65 wt % of the weight of thetotal mixture.

After formation of the organic complex on the support the support mayand preferably is dried to remove most of the solvent and/or waterpresent during formation of the complex. Drying may be achieved underambient conditions such as room temperature or this may be achieved atelevated temperatures, preferably drying is at a temperature from 100 to150° C. Preferably, little or no decomposition of the organic complexoccurs during the drying phase and drying merely results in the removalof non-complexed volatile materials.

The second step in the process of the present invention for themanufacture of a hydrogenation catalyst is the decomposition of theorganic complex on the support, which may be partial or fulldecomposition at this stage. Although not wishing to be bound by anytheory it is believed that this decomposition results in the formationin-situ of one or more precursors to the catalytically active metalsites. It is believed that it is, in part, the formation of theseprecursors and their treatment with hydrogen that ensures that the finalcatalyst exhibits a high degree of catalytic activity and has highlevels of metal dispersion within the catalyst. The hydrogen may be usedin a further step after full or partial decomposition or the full orpartial decomposition may be undertaken in the presence of hydrogenunder pyrolysis conditions. An important parameter in the activity ofcatalytically active metals is the form of the metal on the support andthe level of dispersion of the metal on the support. The process of thepresent invention produces hydrogenation catalysts that comprisecatalytically active metal particles that are relatively small andhighly dispersed. In addition the level of dispersion is relativelystable.

Chemisorption measurements are commonly used to estimate the size ofsupported metal catalysts and metal surface area. The general method formeasuring metal surface area by chemisorption is described in J.Lemaitre et al., “Characterization of Heterogenous Catalysts”, edited byFrancis Delanney, Marcel Dekker, New York (1984), pp. 31.0-324. Thetotal metal surface area on the catalyst is preferably from 0.01 to 10m²/g, particularly preferably from 0.05 to 5 m²/g and more preferablyfrom 0.05 to 3 m²/g of the catalyst. From chemisorption measurements,the % dispersion (% of metal atoms that populate the surface of themetal particles) can be estimated since a properly chosen titrant usedin the chemisorption measurements adsorbs only on metal atoms populatingthe surface. Consequently higher dispersion values indicate smallerparticles with more of the metal atoms populating the surface. For manyhydrogenation reactions, activity correlates with dispersion. Thepreferred method for determining metal dispersion is by using hydrogenas the chemisorption probe molecule under high vacuum static conditionsas follows. The sample is held at a temperature of 40° C. and an 8-pointisotherm (with pressures between 80 and 400 torr) is obtained using H₂as the chemisorption probe molecule. The linear portion of this isothermis extrapolated to zero pressure to obtain the total quantity ofhydrogen chemisorbed; this is the combined dispersion. The sample isthen evacuated at 40° C. to remove any weakly adsorbed hydrogen and thetitration repeated to determine what is referred to as weak adsorptionisotherm. The linear portion of this weak adsorption isotherm isextrapolated to zero pressure to obtain the quantity of weaklychemisorbed hydrogen. Subtraction of these two values for combineddispersion and weak dispersion yields the strongly held chemisorbedquantity. Thus this method provides values for the total metaldispersion, the dispersion due to weakly chemisorbed hydrogen anddispersion due to strongly chemisorbed hydrogen. The value for thestrongly chemisorbed hydrogen is an accurate indication of metaldispersion. In many prior art references the metal dispersion figuresprovided are based on the total chemisorbed probe and are not split intostrong and weak components. In the present invention it is preferredthat the hydrogenation catalysts used have dispersion values relating tothe strongly chemisorbed component in excess of 20% more preferably inexcess of 25% and most preferably in excess of 30%. In addition totaldispersion values in excess of 45% preferably in excess of 50%, morepreferably in excess of 55%, and most preferably in excess of 60% areachieved. Preferably 40% or more of the total metal dispersion relatesto the strongly chemisorbed component, more preferably 45% or more andmost preferably 50% or more.

In the second step of the process for preparing the hydrogenationcatalyst the organic complex is decomposed at least partially or fullydecomposed. In the context of the present invention “partialdecompositions” means that the chemical composition of the organiccomplex is varied; this may be due to a change in the structure of theorganic complex or may be due to the chemical destruction of part of ora component of the complex. When the destruction is partial the methodof destruction is selected to ensure that the removal of non-metalchemical species associated with the complex is incomplete. When thedestruction is complete the only significant element of the complexremaining would be the one or more catalytically active metals as oxideswhen destruction is carried out under oxidizing conditions or thereduced metal when the destruction is carried out in the presence ofhydrogen. There may also be residues such as carbon residues formed fromdecomposition of the organic complex. The partial decomposition is dueto variations in structure and/or composition that do not normally occurunder the drying conditions typically used in catalyst preparationmethods. The changes of structure and/or composition under theconditions of the second stage may be detected and monitored usingvarious analytical techniques that are well known in the art such asinfra-red spectroscopy, mass spectroscopy, thermogravimetric analysis,gas or liquid chromatography and spectroscopy.

A variety of methods may be used to induce partial or full destructionof the organic complex. These include chemical methods such aschemically induced hydrolysis or decomposition such as by the treatmentwith acid or base or ozone or similar chemical active materials. Othermethods for inducing full or partial decomposition include thermalmethods such as pyrolysis and/or calcination, both of which are thepreferred methods with particular preference being given to calcination.A further method is treatment with steam. In one embodiment thepyrolysis may be carried out in the presence of hydrogen; in thisembodiment any subsequent treatment with hydrogen may be omitted.

When calcination or pyrolysis is used as the method for full or partialdecomposition of the organic complex the exact conditions used willdepend on the nature of the complex and especially its thermal stabilityand decomposition profile under elevated temperature. By usingthermogravimetric methods or mass spectroscopy linked with controlledthermal decomposition of the organic complex it is possible to determineat what temperature either under calcination conditions or pyrolysisconditions that initial decomposition and total decomposition of theorganic complex occurs. This indicates the temperature range at whichthis partial decomposition stage should be undertaken or the minimumtemperature that should be selected of full decomposition is required.Alternatively when analysed by infra-red transmission spectroscopy itmay be determined at what point in the treatment that a certainfunctional group is either removed from or formed in the organiccomplex; the temperature at which this occurs if below the totaldecomposition temperature may be selected as the temperature for thepartial decomposition or if above the total decomposition temperaturemay be selected as the temperature for full decomposition. In the casewhere amines are used as the organic compound the temperature belowwhich significant quantities of nitrogen oxides are produced may beselected as the temperature for treatment to induce partialdecomposition. For other organic compounds it may be the temperature atwhich CO or CO₂ are removed from the complex. In the case of amines andespecially amines containing hydroxyl groups or amino acids as theorganic compound it may be the formation of new vibration bands thatappear in the infra-red spectra at between 2100-2200 cm⁻¹ andtentatively assignable to complex carbon nitrogen species such asnitrites and isonitriles being present in the partially decomposedorganic complex. Another method that may be used is where TGA analysisshows total weight loss of the organic complex; temperatures below totalweight loss may be selected for partial decomposition and temperaturesat or above the temperature for total weight loss may be selected forfull decomposition.

When calcination is used to partially or fully decompose the organiccomplex the calcination temperatures used are typically within the rangeof 200 to 1000° C., preferably from 250 to 600° C. The exact temperatureused will depend on whether or not full or partial decomposition of theorganic complex is desired and will depend on the nature of the organiccomplex. Factors that may affect the decomposition temperature of theorganic metal complex include the nature of the metal and/or organiccompound within the complex. Another factor may be the nature of thecounter-ion present when the metal is introduced in the form of a salt.Preferably when partial decomposition is required the support with theorganic complex deposited thereon is calcined at a temperature that isless than the temperature as determined by TGA in air, at which totalweight loss of the organic complex occurs. Preferably it is between 200°C. and the temperature at which total weight loss of the organic complexoccurs. Preferably when full decomposition is required the support withthe organic complex deposited thereon is calcined at a temperature thatis at or above the temperature, as determined by TGA, at which totalweight loss of the organic complex occurs. Preferably it is between thetemperature at which total weight loss of the organic complex occurs and1000° C. Under calcination conditions oxygen is present either as acomponent of an otherwise inert diluent or as a consequence ofcalcination being undertaken in air. When pyrolysis is used thepyrolysis may be undertaken in an inert atmosphere free of oxygen or ina hydrogen atmosphere that may be and preferably is free of oxygen. Whenpyrolysis is used the organic complexes may decompose at highertemperatures than those observed under calcinations conditions. As withcalcination the temperature, under pyrolysis conditions, for partial orfull decomposition may be determined using a variety of methods of whichTGA is preferred. Preferably when partial decomposition is requiredunder pyrolysis conditions in an inert atmosphere or under hydrogen, thesupport with the organic complex deposited thereon is pyrolysed in aninert atmosphere or under hydrogen at a temperature that is less thanthe temperature as determined by TGA in an inert atmosphere or underhydrogen, at which total weight loss of the organic complex occurs.Preferably it is between 200° C. and the temperature at which totalweight loss of the organic complex occurs under pyrolysis conditions inan inert atmosphere or under hydrogen. Preferably when fulldecomposition is required the supports with the organic complexdeposited thereon are pyrolysed at a temperature that is at or above thetemperature, as determined by TGA, at which total weight loss of theorganic complex occurs under pyrolysis conditions in an inert atmosphereor under hydrogen. Preferably it is the between the temperature, underpyrolysis conditions in an inert atmosphere or under hydrogen, at whichtotal weight loss of the organic complex occurs and 1000° C. Preferablythe supports with the organic complex deposited thereon are pyrolysed innitrogen or hydrogen at a temperature of less than 1000° C. The supportcomprising organic complex may be calcined or pyrolysed at the partialdecomposition temperature for a period of time that is sufficient toensure the partial decomposition of the organic complex occurs.Typically this will be for a period of at least 20 minutes, preferablyat least 30, more preferably at least 45 mins and most preferably for 1hour or more. Typically the period of time is 48 hours or less,preferably 24 hours or less and most preferably 12 hours or less. Whenfull decomposition is required the support comprising organic complexmay be calcined or pyrolysed at the full decomposition temperature for aperiod of time that is sufficient to ensure the full decomposition ofthe organic complex.

After the partial or full decomposition of the organic complex thesupport comprising the partially or fully decomposed complex may betreated with a source of hydrogen. This may be omitted when the initialdecomposition is undertaken in the presence of hydrogen. In a preferredembodiment this treatment is undertaken using conditions and methodsnormally used for the activation of hydrogenation catalysts. Theseconditions and methods are selected to ensure that catalytically activemetal is converted to the catalytically active form. In one embodimentthe treatment with hydrogen is carried out by contacting the supportcomprising fully or partially decomposed complex with a gas streamcomprising free hydrogen at from 30 to 600° C., preferably from 100 to550° C., even more preferably from 200 to 500° C., and most preferablyfrom 200 to 450° C. The gas stream preferably consists of from 50 to100% by volume of H₂ and from 0 to 50% by volume of N₂. The treatmentmay be carried our under a continuous flow of hydrogen under atmosphericpressure or under static conditions at elevated pressures up to 100 bar,preferably 1 to 90 bar, more preferably 1 to 20 bar. The activation maybe undertaken for a period of up to 48 hours, preferably no more than 36hours, more preferably less than 24 hours, and most preferably from 30mins to 12 hours. In a preferred embodiment the support comprising fullyor partially decomposed complex is exposed to hydrogen at atmosphericpressure and the temperature raised at a rate slower than 5° C. min⁻¹,more preferably slower than 5° C. min⁻¹ and most preferably slower than2° C. min⁻¹ or less to the treatment temperature where hydrogentreatment is continued for a further 1 to 10 hours, preferably 2 to 8hours and most preferably 3 to 6 hours. When the organic complex hasbeen partially decomposed the exact temperature and time are selected toensure that under hydrogen treatment any residual partially decomposedorganic complex is removed. Therefore the hydrogen treatment temperatureis generally higher than the decomposition temperature of the organiccomplex and the especially the partially decomposed organic complex.

If a plurality of active metals are to be applied to the support and theapplication is carried out in succession, the various process stages ofthe present invention may be repeated in order to deposit each metal insequence.

The total metal surface area on the catalyst is preferably from 0.01 to10 m²/g, particularly preferably from 0.05 to 5 m²/g and more preferablyfrom 0.05 to 3 m²/g of the catalyst. The metal surface area may bemeasured by the chemisorption method as herein described.

In the hydrogenation process of the present invention the hydrogenationconditions are selected taking into account the nature of the organiccompound to be hydrogenated. Generally the hydrogenation process iscarried out at from about 50 to 250° C., preferably from about 70 to220° C., most preferably 75 to 200° C., and more preferably at greaterthan 80° C. The most preferred temperature range is from 80 to 200° C.The pressures used here are generally above 10 bar, preferably fromabout 30 to about 300 bar, and most preferably greater than 50,preferably greater than 75 bar and more preferably from 50 to 220 bar,especially 75 to 220 bar.

The process of the present invention may be carried out eithercontinuously or batchwise, with preference being given to carrying outthe process continuously.

When the process is carried out continuously and the organic compound tobe hydrogenated is a benzenepolycarboxylic acid or derivative thereof,the amount of the benzenepolycarboxylic acid or derivative thereof to behydrogenated or of the mixture of two or more thereof is preferably fromabout 0.05 to about 3 kg per liter of catalyst per hour, more preferablyfrom about 0.1 to about 2 kg per liter of catalyst per hour, mostpreferably from 0.2 to 1 Kg per liter of catalyst per hour.

As hydrogenation gases, it is possible to use any gases which comprisefree hydrogen and do not contain harmful amounts of catalyst poisonssuch as CO, CO₂, COS, H₂S and amines. For example, waste gases from areformer can be used. Preference is given to using pure hydrogen as thehydrogenation gas.

The hydrogenation of the present invention can be carried out in thepresence or absence of a solvent or diluent, i.e. it is not necessary tocarry out the hydrogenation in solution.

However, preference is given to using a solvent or diluent. Solvents ordiluents, which can be used, are any suitable solvent or diluent. Thechoice is not critical as long as the solvent or diluent used is able toform a homogeneous solution with the benzenepolycarboxylic acid or esterto be hydrogenated. For example, the solvents or diluents can alsocomprise water. Examples of suitable solvents or diluents include thefollowing: straight-chain or cyclic ethers such as tetrahydrofuran ordioxane, and also aliphatic alcohols in which the alkyl radicalpreferably has from 1 to 10 carbon atoms, in particular from 3 to 6carbon atoms. Examples of alcohols, which are preferably used, arei-propanol, n-butanol, i-butanol and n-hexanol. Mixtures of these orother solvents or diluents can likewise be used.

The amount of solvent or diluent used is not restricted in anyparticular way and can be selected freely depending on requirements.However, preference is given to amounts which lead to a 10-70% strengthby weight solution of the benzenepolycarboxylic acid or ester to behydrogenated.

In the process of the present invention it is also possible to use oneor more derivates of benzenepolycarboxylic acids in the unpurified statethat is in the presence of one or more starting materials for theirmanufacture such as for example alcohol in the case of esterderivatives. Also present may be traces of monoester derivatives,un-reacted acid such as phthalic acid, sodium monoester derivatives andsodium salts of the acids. In this aspect the benzenecarboxylic acidderivative is hydrogenated prior to purification and after hydrogenationis then sent to process finishing for stripping, drying and polishingfiltration. In this aspect the benzenecarboxylic acid derivative may bean intermediate feed containing high levels of alcohol in the case ofester derivatives. There may be present 5 to 30% excess alcohol thanthat required to achieve complete esterification of the acid. In oneembodiment there may be an intermediate feed containing 8 to 10 wt %isononyl alcohol in di-isononyl phthalate.

In the process of the present invention the desired products are one ormore cyclohexyl materials derived from the hydrogenation of thecorresponding benzenepolycarboxylic acid or derivatives thereof. Ideallythe benzenepolycarboxylic acid or derivatives thereof are converted tothe desired product with a high degree of selectivity and with themaximum conversion possible of the benzenepolycarboxylic acid orderivatives thereof. Hydrogenations of this type often result inundesirable by-products of relatively low molecular weight and lowboiling point; these by-products are referred to as “lights”. In thecontext of the present invention “lights” are defined as materials inthe as hydrogenated reaction product that are eluted before the objectcyclohexyl materials when the as hydrogenated reaction product isanalyzed by Gas Liquid Chromatography. Details for one suitable methodfor determining the “lights” content of a product obtained by theprocess of the present invention is provided in the specific examples.When using the process of the present invention it is possible to obtaingreater than 95% conversion of the starting material (one or morebenzenepolycarboxylic acid or derivatives thereof), whilst at the sametime producing less than 1.5% by weight based on the total weight ofreaction product of “lights”. In the process of the present inventionthe product obtained directly from the hydrogenation reaction ideallycontains the object cyclohexyl derivative(s) in an amount that equatesto 97 or greater mole % conversion of the starting material, preferably98.5 or greater mole % conversion, more preferably 99 or greater mole %conversion, and most preferably 99.9 or greater mole % conversion. Inthe process of the present invention the product obtained directly fromthe hydrogenation reaction ideally contains 1.3% or less, preferably1.0% or less, more preferably 0.75% or less, even more preferably 0.5%or less, and in the most preferable embodiment less than 0.3% by weightbased on the total weight of the reaction product of “lights”. When ashydrogenated products of this level of purity are obtained it may bepossible to use these materials directly in certain applications withoutthe need for further purification of the as hydrogenated product such asplasticisers for plastics products.

The process of the present invention is further illustrated by means ofthe following examples.

EXAMPLES Example 1 Preparation of MCM-41

A sample of MCM-41 (40 Å) was prepared in accordance with the methoddescribed below, which corresponds to Example 21 of U.S. Pat. No.5,837,639. The following mixture (parts by weight—pbw) was charged to anautoclave:

83.7 pbw Cetyltrimethylammonium (CTMA) hydroxide prepared by contactinga 29 wt. % N,N,N-trimethyl-1-hexadecylammonium chloride solution with ahydroxide-for halide exchange resin, 1.7 pbw sodium aluminate, 41.1 pbwtetramethylammonium silicate (10% aqueous solution), and 10.5 pbwprecipitated hydrated silica (HiSil)

The mixture was crystallized at 100° C. for 20 hours with stirring underautogeneous pressure. The resulting product was recovered by filtrationand dried in air at ambient temperature. The product was then calcinedat 540° C. for one hour in nitrogen, followed by six hours in air. Thecalcined product had a surface area of 1120 m²/g and the followingequilibrium adsorption capacities in gram/100 grams:

H₂O 10.8 Cyclohexane >50 n-Hexane >50 Benzene 67

The product was identified as MCM-41 with an X-ray diffraction patternthat included a very strong relative intensity line at 38.4+/−2.0 Å, andweak lines at 22.6+/−1.0, 20.0+/−1.0, and 15.2+/− Å.

Example 1b Preparation of MCM-41

A sample of MCM-41 (40 Å) was prepared in accordance with the followingmethod:

The following mixture (parts by weight-pbw) was charged to an autoclave:

26.8 pbw distilled water, 3.5 pbw Cetyltrimethylammonium (CTMA) chloride(29 wt. % aqueous solution), 4.55 pbw precipitated hydrated silica(Ultrasil PM), 1 pbw Tetramethylammonium hydroxide (25 wt. % aqueous)

The mixture was crystallized at 150° C. for 20 hours with stirring underautogeneous pressure. The resulting product was recovered by filtrationand dried in air at ambient temperature. The product was then calcinedat 540° C. for one hour in nitrogen, followed by six hours in air. Theproduct was identified as MCM-41. The calcined product has a surfacearea of 903 m²/g and a pore size (determined by nitrogen adsorption) of3.8 nm. The analyses are as follows:

Silica 96.8 wt. % Alumina 0.1018 wt. % Sodium 0.0300 wt. % Carbon 0.11wt. %Sorption capacities were as follows:

H₂O  5.9 wt. % Cyclohexane 53.9 wt. % n-Hexane 44.1 wt. %

Example 2a Preparation of Hydrogenation Catalyst—Ruthenium andMCM-41—TEA/Aqueous Method

A solution was prepared by combining with stirring 16.6 grams ofruthenium (III) nitrosyl nitrate aqueous solution with 25.7 grams oftriethanolamine and 25.7 grams of distilled water. This solution wasadded slowly to 25 grams of MCM-41 of Example 1b and dried overnight at100° C. The catalyst was then calcined to 400° C. for three hours inflowing air. The ruthenium content was a nominal 0.5%.

Example 2b Preparation of Hydrogenation Catalyst—Ruthenium and MCM-41Aqueous Method

A solution was prepared by combining with stirring 16.6 grams ofruthenium (III) nitrosyl nitrate aqueous solution with 51.4 grams ofdistilled water. This solution was added slowly to 25 grams of MCM-41 ofExample 1b and dried overnight at 100° C. The catalyst was then calcinedto 400° C. for three hours in flowing air. The ruthenium content was anominal 0.5%.

Example 3 Reduction of Metal Component of Hydrogenation Catalysts ofExamples 2a and 2b

The catalysts prepared in Examples 2 and 3 were activated under two setsof conditions a) and b) as follows:

a) Catalyst particles (10/20 mesh) were loaded into a stainless-steelcatalyst basket then installed in a 300 cm³ autoclave. Metal reductionwas conducted under a continuous atmospheric hydrogen flow of ˜100 cm³min⁻¹ at 200° C. for 18 hours.

b) Catalyst particles (10/20 mesh) were loaded into a stainless-steelcatalyst basket then installed in a 300 cm³ autoclave. Metal reductionwas conducted under a static hydrogen pressure of 1250 psig (approx 86bar) at 200° C. for 14 hours.

Example 4 Hydrogenation of Di-isononyl phthalate (DINP)

After hydrogen activation the autoclave, containing activated catalyst,was cooled to room temperature and 137.4-194.5 g (0.28-0.46 mol) ofliquid DINP (Jayflex DINP (CAS No. 6851548-0). The autoclave was sealed,heated to hydrogenation temperature of 80 or 120° C., and pressurizedwith hydrogen to either a pressure of 840 psig (approx 58 bar) or 3000psig (approx 207 bar). Hydrogenation was carried out for up to 7 hours.During hydrogenation samples were taken at regular intervals to analyzethe conversion of DINP and assess the level of lights formation.Conversion of DINP was calculated directly based on the peak areas ofresidual aromatic proton resonance in 1H NMR spectra. The lights contentof the sample was determined by Gas Liquid Chromatography using a DB-1column (60 m×0.25 mm×0.25 μm), operated at 40-275° C. at a ramp rate of10° C./min and holding at 275° C. for 35 minutes. The lights weredetermined as being all peaks, which eluted before 24.5 minutes.Components eluted thereafter were considered asCyclohexanedicarboxylates products. The conversions and selectivitiesfor the various hydrogenations are provided in Table 1.

The data in this table indicates that the catalysts prepared viaimpregnation with a triethanolamine/aqueous ruthenium mixture are moreactive hydrogenation catalysts compared with those prepared via aqueousruthenium impregnation without the use of triethanolamine. The data alsoindicates that the catalysts prepared via impregnation with atriethanolamine/aqueous ruthenium mixture produce lower levels of lightsat higher hydrogenation pressures.

A comparison of FIG. 1 and FIG. 2 illustrates that the catalyst preparedaccording to the process of the present invention is significantly moreactive as a hydrogenation catalyst compared to the catalyst prepared viathe conventional aqueous route. These plots of DINP conversion vsreaction time indicate that the DINP hydrogenation followsLangmuir-Hinshelwood kineticsRate=k[DINP]/{1+k′[DINP]+k″[H6−DINP]}

To calculate the k value, only data with <90% DINP was used. At <90 DINPconversion and under constant H₂ pressure, DINP conversion is zero-orderwith respect to DINP concentration. The calculated k values for Examples4 (d) and 4 (e) are 0.41 mole/liter·h and 0.31 mole/liter·h. Thus thecatalyst prepared according to the process of the present invention is32% more active than a catalyst prepared through aqueous impregnation.

Example 5 Hydrogen treatment and Measurement of H Chemisorption Valuesfor Supported Ru Hydrogenation Catalysts of Examples 6 to 14

(A) Activation. Approximately 0.3 to 0.5 grams of catalyst was loaded inthe chemisorption cell, reduced in flowing hydrogen at one atmospheretotal pressure at the temperature indicated in Tables 2 to 6. Thesamples were heated to the final reduction temperature at 2° C./min andheld at this temperature for three hours. After this treatment thecatalyst was activated and ready for use as a hydrogenation catalyst.

(B) The chemisorption measurements were obtained under static highvacuum conditions. After the hydrogen treatment under (A) hydrogen wasthen pumped off under dynamic vacuum for 15-30 minutes at the reductiontemperature indicated in Tables 2 to 6. The temperature was lowered to40° C. and an 8-point isotherm (with pressures between 80 and 400 torr)was obtained using H₂ as the chemisorption probe molecule. The linearportion of this isotherm was extrapolated to zero pressure to obtain thetotal quantity of hydrogen chemisorbed. This is shown in Tables 2 to 6in the column labeled % dispersion (combined). The sample was evacuatedat 40° C. to remove any weakly adsorbed hydrogen and the titrationrepeated to determine the weak adsorption isotherm. The linear portionof this isotherm was extrapolated to zero pressure to obtain thequantity of weakly chemisorbed hydrogen. This is shown in Tables 2 to 6as the column labeled % dispersion (weak). Subtraction of these twovalues yields the strongly held chemisorbed quantity and is shown inaccompanying tables below in the column labeled % dispersion (strong).All values are based on a H/Ru_(surface) ratio of 1.

Example 6 Preparation of Organic Complex Comprising 0.5% Ru on SiO₂Using Aminoalcohol in Impregnation Solution

15.00 g of silica support (S.A=85 m²/g, P.D.=50 nm) was impregnated withsolution prepared by mixing 5.01 g of ruthenium nitrosyl nitrate (1.5%Ru), 2.23 g triethanolamine and 1.77 g water and dried at 100° C. forfour hours.

Example 7 Calcination of Catalyst of Example 6 to 300° C.

A portion of sample from Example 6 was calcined in flowing air as thetemperature was ramped 1° C./minute to 300° C. and held for one hour atthat temperature. A chemisorption measurement was made on this sampleafter hydrogen treatment.

Example 8 Calcination of Catalyst of Example 6 to 400° C.

A portion of sample from Example 6 was further calcined in air at aheating rate of 1° C./min to 400° C. and held at that temperature for 3hours. A chemisorption measurement was made on this sample afterhydrogen treatment.

Table 2 compares the dispersion measurements by H chemisorption of thecatalysts of Examples 7 and 8. This comparison shows that the highestdispersions are obtained when the Ru-TEA on silica catalyst is calcinedat 300° C., which partially decomposes the complex. After 400° C.calcination the organic complex is totally destroyed before hydrogentreatment and it can be seen that the chemisorption values aresubstantially lower and are unstable as they decrease as the reductiontemperature is increased above 250° C. The higher values in the Example7 catalyst remain stable during reduction at 400° C.

Example 9 Preparation of 0.5% Ru on SiO₂ Using Aminoalcohol inImpregnation Solution

25.00 g of silica support (S.A=250 m²/g, P.D.=15 nm) was impregnatedwith solution prepared by mixing 8.37 g of ruthenium nitrosyl nitrate(1.5% Ru), 3.71 g triethanolamine and 18.00 g water and dried at 100° C.for four hours.

Example 10 Calcination of catalyst of Example 9 to 275° C.

A portion of sample from Example 9 was calcined in flowing air as thetemperature was ramped 1° C./minute to 275° C. and held at thattemperature for one hour. A chemisorption measurement was made on thissample after hydrogen treatment.

Example 11 Pyrolyzing Catalyst of Example 9 in Oxygen-Free Environment

A portion of Sample from Example 9 was heated in flowing nitrogen as thetemperature was ramped 2° C./minute to 400° C. and held at thattemperature for one hour. A chemisorption measurement was made on thissample after hydrogen treatment.

Table 3 compares the dispersion measurements by H chemisorption of thecatalysts of Examples 10 and 11. Both treatments generate a remnant ofthe starting Ru-triethanolamine complex. This comparison shows that thepartial decomposition may be achieved at higher temperatures when underinert pyrolysis conditions (absence of oxygen) to form the Ru-organicprecursor that gives high dispersion as well as when produced viaoxidation.

Example 12 Comparative Sample of 0.5% Ru on Silica with no OrganicAdditive

15.00 g of silica support (S.A=85 m²/g, P.D.=50 nm) was impregnated withsolution prepared by mixing 5.00 g of ruthenium nitrosyl nitrate (1.5%Ru) and 4.00 g water and dried at 100° C. for four hours. Achemisorption measurement was made on this sample after hydrogentreatment.

Example 13 Comparative Sample of 0.5% Ru on Silica with no OrganicAdditive and Calcination

15.00 g of silica support (S.A=85 m²/g, P.D.=50 nm) was impregnated withsolution prepared by mixing 5.00 g of ruthenium nitrosyl nitrate (1.5%Ru) and 4.00 g water and dried at 100° C. for four hours. The sample wasthen calcined in air as the temperature was ramped 1° C./minute to 300°C. and held at that temperature for one hour. A chemisorptionmeasurement was made on this sample after hydrogen treatment.

Table 4 compares the dispersion measurements by H chemisorption of thecatalysts of Examples 7, 12 and 13. Only the catalyst prepared accordingto Example 7 in the Table is an object of this invention and has theremnant of the starting Ru-triethanolamine complex. This comparisonshows that a high initial dispersion can be obtained on a catalyst thatis simply impregnated with an aqueous solution of the Ruthenium salt andthen dried at low temperature if it is reduced at temperatures as low as150° C. On reduction at higher temperatures the dispersion numbersdecrease dramatically, most probably as a result of sintering. This doesnot happen with the catalyst of Example 7, which remains stable at 400°C. reduction temperatures. If the aqueous salt solution of Ru iscalcined first to 300° C. the dispersion numbers are very low (Example13).

Example 14 Preparation of 0.5% Ru on SiO₂ Using Aminoacid inImpregnation Solution

10.00 g of silica support (S.A=85 m²/g, P.D.=50 nm) was impregnated withsolution prepared by mixing 3.34 g of ruthenium nitrosyl nitrate (1.5%Ru), 0.70 g L-arginine, and enough water to form a total 10 cc solutionvolume. The sample was dried at 100° C. for four hours and thetemperature was then ramped 1° C./minute to 250° C. and held at thattemperature for one hour. A chemisorption measurement was made on thissample after hydrogen treatment.

Table 5 compares the dispersion measurements by H chemisorption of thecatalysts of Examples 7 and 14. Both calcined samples leave a remnant ofthe starting Ru-amino complexes. This comparison shows that highdispersions are obtained when using either aminoalcohols or aminoacidsin the impregnation solution.

The data Table 6 shows the chemisorption data for Examples 9 and 10.This comparison shows that the dried catalyst with the amino complex(Example 9) gives a good dispersion value if directly reduced inhydrogen that is superior to the sample where the complex is completelyoxidized to remove the complex (Example 8 see Table 2). However, thedispersion is not as good as that obtained if the organic complex iseither partially oxidized or pyrolysed.

Example 16 Measurement of Decomposition Products of Catalyst PrecursorFormed by Partial Oxidation of Ru-Triethanolamine Complex

A portion of the catalyst from Example 7 was heated in air at 4 deg/minand the product gas was analyzed by a quadrapole mass spectrometer. Thedata is shown in FIG. 3. FIG. 3 shows that a water peak is releasedslightly below 200° C. and then there is formation of CO₂, NO₂ and H₂Oas the organic complex is completely oxidized near to 350° C. This showsthat the complex contained C, N and H. There might be O as well but wecannot tell from this experiment as it is carried out under oxidizingconditions.

Example 17 Infra-Red Spectroscopy

The samples containing partially decomposed organic complex derived fromRu-triethanolamine and Ru-arginine were also analyzed using infraredspectroscopy. Approximately 25 mg of the materials of Example 7, (TEA,calc 300° C.), Example 12 (no organic, dry 100° C.) and Example 14(L-arginine, calc 250 C) were separately formed into 13 mm pellets andloaded into an IR spectrometer operating in transmission mode. Thesamples were heated in vacuum to 150° C. before the spectra wereobtained.

The data are shown in FIG. 4. The data shows the plot of transmittancevs. wave number of the IR radiation. The transmittance decreases wherethe catalyst absorbs infrared radiation due to a characteristicstretching of a molecular species. The peaks between 1500 and 2000 cm⁻¹are primarily silica stretching bands. The presence of absorptionfeatures around 2100-2200 cm⁻¹, present on samples from Examples 7 and14 are reported to be features of complexed carbon nitrogen species suchas nitrites and isonitriles (see: Infrared and Raman Spectra ofInorganic and Coordination Compounds, by K. Nakamoto, John Wileypublishers, 3rd edition, 1978; ISBN: 0-471-62979-0 pages 267-269). Thepeaks are absent on the starting silica as well as on the sampleprepared by aqueous impregnation of the ruthenium complex with no aminoalcohol or amino acids present. Consequently these peaks are anindication of the remnant of the starting Ru-triethanolamine andRu-arginine complexes present after partial decomposition of the organiccomplex.

Example 18 Thermogravimetric Analysis

FIG. 5 shows the air treatment TGA plot for a catalyst sample (0.5 wt %Ru on SiO₂), which had been prepared with triethanolamine as the organiccompound and dried at 100° C. prior to analysis. The TGA plot showsweight loss at temperatures below 300° C. due to loss of water andpartial oxidation of the complex with triethanolamine. In addition thereis a further weight loss at approximately 325° C., which is believed tobe due to the complete oxidation of the organic complex.

FIG. 6 shows the air treatment TGA plot for a similar catalyst to thatused in FIG. 1 (0.5 wt % Ru on SiO₂), which had previously been calcinedat 300° C. Clearly there is an insignificant weight loss below 300° C.;this is due to the fact that any material on the supported catalyst thatwould have been removed below this temperature has been removed by thecalcination. The majority of the weight loss in the sample is due to thepartially decomposed organic complex, which is oxidized at approximately325° C. This results shows that that calcination below the decompositiontemperature is necessary to form the partially decomposed organiccomplex.

FIG. 7 shows the hydrogen treatment TGA for the catalyst sample (0.5 wt% Ru on SiO₂), which had previously been calcined at 300° C. This TGAanalysis shows that the partially oxidised organic complex is fullydecomposed under the hydrogen treatment conditions at a highertemperature (˜400° C.) than under calcination conditions.

Example 19 Preparation of 20% Ni/Al₂O₃ Conventional Preparation

20 grams of reforming grade gamma Al₂O₃ with a surface area of 190 m2/g, was impregnated by incipient wetness with 12 cc of an aqueousimpregnation solution containing 24.8 g of nickel nitrate hexahydrate.After being dried at 120° C., the sample was calcined at 350° C. forfour hours.

Example 20 Preparation of 20% Ni/Al₂O₃ with DMEA Post-Treat on DriedImpregnate

20 grams of reforming grade gamma Al₂O₃ with a surface area of 190 m2/g, was impregnated by incipient wetness with 12 cc of an aqueousimpregnation solution containing 24.8 g of nickel nitrate hexahydrate.After being dried at 120° C., the sample was re-impregnated to incipientwetness with a 10.6 cc of an aqueous solution containing 7.6 grams ofN,N-dimethylethanolamine. The sample was then dried at 120° C. overnightand then calcined at 350° C. for 4 hours. Under these conditions theorganic complex was fully decomposed

The dispersions of Ni the catalysts of Examples 19 and 20 was determinedvia a hydrogen chemisorption technique. The results are provided inTable 7. These results show a dramatic increase in Ni dispersion whenthe NI is deposited using the process of the present invention.

TABLE 7 Hydrogen Sample chemisorption Ni/Al₂O₃ Treatment H/Ni in %Example 19 No post-treat nor additions to 8.3 impregnation solutionExample 20 N,N dimethylethanolamine post-treat 11.6 driedimpregnate/oxidize

TABLE 1 Example H₂ Metal Weight Weight Temp Pressure Time ConversionLights No Catalyst Activation Deposition DINP (g) Catalyst (g) (° C.)(psig) (h) (%) (%) 4 (a) 0.5 wt % Ru Ex 3 (a) Ex 2 (a) 137.4 6.87 120°C. 3000 3 99.9 0.35 MCM-41 4 (b) 0.5 wt % Ru Ex 3 (a) Ex 2 (a) 118.25.91  80° C. 3000 3 73.6 0.32 MCM-41 4 (c) 0.5 wt % Ru Ex 3 (a) Ex 2 (b)138.4 6.92  80° C. 3000 3 37.9 0.16 (comp) MCM-41 (Comp) 4 (d) 0.5 wt %Ru Ex 3 (b) Ex 2 (a) 194.5 10 120° C. 840 7.5 99.6 0.44 MCM-41 4 (e) 0.5wt % Ru Ex 3 (b) Ex 2 (b) 190.5 10 120° C. 840 7.5 93.7 1.22 (Comp)MCM-41 (Comp) Comp = comparative example

TABLE 2 Sample of 0.5% Ru Supported on Reduction % dispersion %dispersion % dispersion SiO₂ temperature (combined) (weak) (strong)Example 7 250 0 0 0.0 Ru-TEA/ 325 0 0 0.0 300° C. 400 63.1 28.9 34.1 40066.4 29.7 36.7 400 65.8 28.6 37.3 400 65.8 29.0 36.9 Example 8 250 16.187 9.2 Ru-TEA/ 325 9.46 3.97 5.5 400° C. 400 8.69 1.67 7.0 400 6.66 0 6.7

TABLE 3 Sample of 0.5% Ru Supported on Reduction % dispersion %dispersion % dispersion SiO₂ temperature (combined) (weak) (strong)Example 10 250 0 0 0.0 Ru/TEA/ 325 0 0 0.0 275° C. 400 57.6 29.9 27.7air 400 55.3 31.7 23.6 Example 11 250 0 0 0.0 Ru/TEA/ 325 0 0 0.0 400°C. 400 52.8 25.9 26.9 N₂ 400 60.8 30.6 30.2 400 64.6 31.4 33.2 400 64.731.5 33.2

TABLE 4 Sample of 0.5% Ru Supported on Reduction % dispersion %dispersion % dispersion SiO₂ temperature (combined) (weak) (strong)Example 7 250 0 0 0.0 Ru-TEA/ 325 0 0 0.0 300° C. 400 63.1 28.9 34.1 40066.4 29.7 36.7 400 65.8 28.6 37.3 400 65.8 29.0 36.9 Example 12 15077.77 40.87 36.9 Ru-aq/ 200 72.68 38.24 34.4 100° C. 250 66.54 36.5130.0 325 53.99 32.64 21.4 400 45.98 27.67 18.3 400 43.65 27.2 16.5 40042.64 25.84 16.8 Example 13 250 1.22 0 1.2 Ru-aq/ 325 0.38 0 0.4 300° C.400 0.23 0 0.2

TABLE 5 Sample of 0.5% Ru Supported on Reduction % dispersion %dispersion % dispersion SiO₂ temperature (combined) (weak) (strong)Example 7 250 0 0 0.0 Ru-TEA/ 325 0 0 0.0 300° C. 400 63.1 28.9 34.1 40066.4 29.7 36.7 400 65.8 28.6 37.3 400 65.8 29.0 36.9 Example 14 250 0 00.0 Ru-arginine/ 325 0 0 0.0 250° C. 400 65.09 33.4 31.7 400 68.91 34.4234.5

TABLE 6 Sample of 0.5% Ru Supported on Reduction % dispersion %dispersion % dispersion SiO₂ temperature (combined) (weak) (strong)Example 9 250 0 0 0.0 Ru/TEA/dry 400 48.87 30.02 18.9 100 C. air 40049.79 29.3 20.5 400 49.86 30.55 19.3 Example 10 250 0 0 0.0 Ru/TEA/ 3250 0 0.0 275° C. 400 57.6 29.9 27.7 air 400 55.3 31.7 23.6

1. A process comprising: (a) contacting one or morebenzenepolycarboxylic acids or a mixture of one or morebenzenepolycarboxylic acids with a source of hydrogen in the presence ofa catalyst comprising one or more catalytically active metal siteslocated on a catalyst support, under hydrogenation conditions, wherebyat least one of said one or more benzenepolycarboxylic acids or mixtureof one or more benzenepolycarboxylic acids are hydrogenated to provide aproduct; (b) recovering said product; wherein at least one of saidcatalytically active metal sites has been obtained via the partialdecomposition on said catalyst support of a complex of a TransitionGroup VIII metal and a compound selected from the group consisting of(i) amino acids and (ii) aliphatic amines comprising one or morehydroxyl groups, partial decomposition having been carried out such thatnew vibration bands appear in the infra red spectrum of the complex atbetween 2100-2200 cm⁻¹ and (a) having been carried out in the presenceof hydrogen or (b) being followed by treatment with hydrogen.
 2. Theprocess according to claim 1, wherein said benzenepolycarboxylic acid isselected from the group consisting of phthalic acid, terephthalic acid,isophthalic acid, trimellitic acid, trimesic acid, hemimellitic acid andpyromellitic acid, and mixtures of two or more thereof.
 3. The processaccording to claim 1, wherein said benzenepolycarboxylic acid isselected from the group consisting monoalkyl and dialkyl esters ofphthalic acid, terephthalic acid and isophthalic acid, monoalkyl,dialkyl and trialkyl esters of trimellitic acid, trimesic acid andhemimellitic acid, monoalkyl, dialkyl, trialkyl and tetraalkyl esters ofpyromellitic acid, where the alkyl groups can be linear or branched andeach have from 3 to 18 carbon atoms, anhydrides of phthalic acid,trimellitic acid and hemimellitic acid, pyromellitic dianhydride, andmixtures of two or more thereof.
 4. The process according to claim 1,wherein said contacting in step (a) is carried out at a pressure of 25to 300 bar.
 5. The process according to claim 1, wherein said contactingin step (a) is carried out at a pressure of 50 to 220 bar.
 6. Theprocess according to claim 1, wherein the total metal dispersion of thehydrogenation catalyst is 45% or more and the metal dispersion relatingto a strongly chemisorbed component of the total metal dispersion is2000 or greater.
 7. The process according to claim 1, wherein saiddecomposition is undertaken under hydrogen.
 8. The process according toclaim 1, wherein after decomposition the partially or fully decomposedorganic complex is treated with a source of hydrogen.
 9. The processaccording to claim 1, wherein said decomposition is undertaken viacalcination, and said calcination temperature is less than thetemperature, as determined by TGA in air, at which total weight loss ofthe organic complex occurs.
 10. The process according to claim 9,wherein said calcination temperature is between 200° C. and thetemperature at which total weight loss of the organic complex occurs.11. The process according to claim 1, wherein at least one of saidsupport materials is one or more ordered mesoporous materials.
 12. Theprocess according to claim 11, wherein at least one of said supportmaterials are selected from the group consisting of MCM-41, MCM-48 andMCM-50.
 13. The process according to claim 1, wherein said Group VIIImetal is selected from the group consisting of platinum, rhodium,palladium, cobalt, nickel, ruthenium and a mixture of two or morethereof.
 14. A process for hydrogenating one or morebenzenepolycarboxylic acids comprising: (a) contacting one or morebenzenepolycarboxylic acids with a source of hydrogen in the presence ofa catalyst comprising one or more catalytically active metal siteslocated on a catalyst support, under hydrogenation conditions, wherebysaid one or more benzenepolycarboxylic acids are hydrogenated to providea product; (b) recovering said product; wherein at least one of saidcatalytically active metal sites has been obtained via the partialdecomposition on said catalyst support of a complex of a TransitionGroup VIII metal and a compound selected from the group consisting of(i) amino acids and (ii) aliphatic amines having one or more hydroxylgroups, partial decomposition having been carried out such that newvibration bands appear in the infra red spectrum of the complex atbetween 2100-2200 cm⁻¹ and (a) having been carried out in the presenceof hydrogen or (b) being followed by treatment with hydrogen; whereinsaid Transition Group VIII metal is selected from the group consistingof platinum, rhodium, palladium, cobalt, nickel, ruthenium and a mixtureof two or more thereof; and wherein at least one of said supportmaterials are selected from the group consisting of silica, MCM-41,MCM-48 and MCM-50.
 15. The process of claim 1, wherein the aliphaticamines comprises one or more hydroxyalkyl groups.
 16. The process ofclaim 15, wherein the hydroxyalkyl groups are selected from the groupsconsisting of C₁-C₅₀-hydroxyalkyl groups, C₁-C₈-hydroxyalkyl groups, andC₁-C₄ hydroxyalkyl groups.
 17. The process of claim 15, wherein thehydroxyalkyl groups are selected from one or more of the followinggroups: hydroxymethyl, 1-hydroxyethyl, 2-hydroxyethyl,1-hydroxy-n-propyl, 2-hydroxy-n-propyl, 3-hydroxy-n-propyl, and1-hydroxy-methyl-ethyl.
 18. The process of claim 1, wherein thealiphatic amine has one or more mono-, di-, and tri-, substitutedaliphatic hydroxyalkylamines.
 19. The process of claim 1, wherein thealiphatic amine is selected from the group consisting of methanolamine,di-methanolamine, tri-methanolamine, ethanolamine, di-ethanolamine,tri-ethanolamine, butanolamine, di-butanolamine, tri-butanolamine,propanolamine, di-propanolamine, and tri-propanolamine.
 20. The processof claim 14, wherein the aliphatic amines have one or more hydroxyalkylgroups.
 21. The process of claim 20, wherein the hydroxyalkyl groups areselected from the groups consisting of C₁-C₅₀-hydroxyalkyl groups,C₁-C₈-hydroxyalkyl groups, and C₁-C₄ hydroxyalkyl groups.
 22. Theprocess of claim 20, wherein the hydroxyalkyl groups are selected fromone or more of the following groups: hydroxymethyl, 1-hydroxyethyl,2-hydroxyethyl, 1-hydroxy-n-propyl, 2-hydroxy-n-propyl,3-hydroxy-n-propyl, and 1-hydroxy-methyl-ethyl.
 23. The process of claim14, wherein the aliphatic amine has one or more mono-, di-, and tri-,substituted aliphatic hydroxyalkylamines.
 24. The process of claim 14,wherein the aliphatic amine is selected from the group consisting ofmethanolamine, di-methanolamine, tri-methanolamine, ethanolamine,di-ethanolamine, tri-ethanolamine, butanolamine, di-butanolamine,tri-butanolamine, propanolamine, di-propanolamine, andtri-propanolamine.
 25. A process comprising: (a) contacting one or morebenzenepolycarboxylic acids or a mixture of one or morebenzenepolycarboxylic acids with a source of hydrogen in the presence ofa catalyst comprising one or more catalytically active metal siteslocated on a catalyst support, under hydrogenation conditions, wherebyat least one of said one or more benzenepolycarboxylic acids or amixture of one or more benzenepolycarboxylic acids are hydrogenated toprovide a product; (b) recovering said product; wherein at least one ofsaid catalytically active metal sites has been obtained via the partialdecomposition on said catalyst support of a complex of a TransitionGroup VIII metal and a compound selected from the group consisting of(i) amino acids and (ii) a compound represented by the formula:NR¹R²R³ wherein R¹ and R² are independently hydrogen, or R¹, R² and R³independently are one or more of the following groups: C₁-C₅₀-alkyl,C₃-C₅₀-cycloalkyl, aromatic, C₁-C₅₀-alkyl substituted aromatic,C₁-C₅₀-hydroxyalkyl, amino- and/or hydroxyl-substituted C₁-C₅₀-alkyl,C₂-C₅₀-alkoxyalkyl, C₃-C₅₀-dialkylaminoalkyl, C₂-C₅₀-alkylaminoalkyl,C₁-C₅₀-alkyl substituted heterocyclic and aromatic heterocycliccompounds, and C₁-C₅₀-alkylene moieties substituted with one or morearomatic groups, optionally, R¹ and R² may form, with the nitrogen atom,a nitrogen-containing heterocycle, aromatic heterocycle, alkylsubstituted heterocycle, or alkyl substituted aromatic heterocycle;partial decomposition having been carried out such that new vibrationbands appear in the infra red spectrum of the complex at between2100-2200 cm⁻¹ and (a) having been carried out in the presence ofhydrogen or (b) being followed by treatment with hydrogen.
 26. Theprocess of claim 25, wherein said Transition Group VIII metal isselected from the group consisting of platinum, rhodium, palladium,cobalt, nickel, ruthenium and a mixture of two or more thereof.
 27. Theprocess of claim 26, wherein at least one of said support materials areselected from the group consisting of MCM-41, MCM-48 and MCM-50.
 28. Theprocess of claim 1, wherein the catalyst support comprises silica. 29.The process of claim 28, wherein the silica is amorphous.
 30. Theprocess of claim 25, wherein the catalyst support comprises silica. 31.The process of claim 30, wherein the silica is amorphous.
 32. Theprocess of claim 14, wherein the silica is amorphous.